US10617974B2 - Method and apparatus for extracting botanical oils - Google Patents

Method and apparatus for extracting botanical oils Download PDF

Info

Publication number
US10617974B2
US10617974B2 US16/098,265 US201716098265A US10617974B2 US 10617974 B2 US10617974 B2 US 10617974B2 US 201716098265 A US201716098265 A US 201716098265A US 10617974 B2 US10617974 B2 US 10617974B2
Authority
US
United States
Prior art keywords
gas stream
oil
plant material
solvent
temperature
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
US16/098,265
Other languages
English (en)
Other versions
US20190151771A1 (en
Inventor
C. Russell Thomas
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Natural Extraction Systems LLC
Original Assignee
Natural Extraction Systems LLC
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Natural Extraction Systems LLC filed Critical Natural Extraction Systems LLC
Priority to US16/098,265 priority Critical patent/US10617974B2/en
Assigned to Natural Extraction Systems, LLC reassignment Natural Extraction Systems, LLC ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: THOMAS, C. RUSSELL
Assigned to Natural Extraction Systems, LLC reassignment Natural Extraction Systems, LLC ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: THOMAS, C. RUSSELL
Publication of US20190151771A1 publication Critical patent/US20190151771A1/en
Application granted granted Critical
Publication of US10617974B2 publication Critical patent/US10617974B2/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D11/00—Solvent extraction
    • B01D11/02—Solvent extraction of solids
    • B01D11/0292—Treatment of the solvent
    • B01D11/0296—Condensation of solvent vapours
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/14—Evaporating with heated gases or vapours or liquids in contact with the liquid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D11/00—Solvent extraction
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
    • B01D3/343—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances the substance being a gas
    • B01D3/346—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances the substance being a gas the gas being used for removing vapours, e.g. transport gas
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
    • B01D3/38—Steam distillation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
    • B01D3/40—Extractive distillation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
    • B01D45/12—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0003—Condensation of vapours; Recovering volatile solvents by condensation by using heat-exchange surfaces for indirect contact between gases or vapours and the cooling medium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0033—Other features
    • B01D5/0042—Thermo-electric condensing; using Peltier-effect
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0057—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes
    • B01D5/0072—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes with filtration
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C37/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring
    • C07C37/68—Purification; separation; Use of additives, e.g. for stabilisation
    • C07C37/685—Processes comprising at least two steps in series
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C37/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring
    • C07C37/68—Purification; separation; Use of additives, e.g. for stabilisation
    • C07C37/70—Purification; separation; Use of additives, e.g. for stabilisation by physical treatment
    • C07C37/72—Purification; separation; Use of additives, e.g. for stabilisation by physical treatment by liquid-liquid treatment
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07D—HETEROCYCLIC COMPOUNDS
    • C07D311/00—Heterocyclic compounds containing six-membered rings having one oxygen atom as the only hetero atom, condensed with other rings
    • C07D311/02—Heterocyclic compounds containing six-membered rings having one oxygen atom as the only hetero atom, condensed with other rings ortho- or peri-condensed with carbocyclic rings or ring systems
    • C07D311/78—Ring systems having three or more relevant rings
    • C07D311/80—Dibenzopyrans; Hydrogenated dibenzopyrans
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
    • C11B1/00—Production of fats or fatty oils from raw materials
    • C11B1/10—Production of fats or fatty oils from raw materials by extracting
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D11/00—Solvent extraction
    • B01D11/02—Solvent extraction of solids
    • B01D11/028—Flow sheets
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D11/00—Solvent extraction
    • B01D11/02—Solvent extraction of solids
    • B01D11/0288—Applications, solvents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D11/00—Solvent extraction
    • B01D11/02—Solvent extraction of solids
    • B01D11/0292—Treatment of the solvent
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D11/00—Solvent extraction
    • B01D2011/007—Extraction using a solvent in the gas phase
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
    • B01D45/12—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces
    • B01D45/16—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces generated by the winding course of the gas stream, the centrifugal forces being generated solely or partly by mechanical means, e.g. fixed swirl vanes

Definitions

  • the present invention consists of a system of parts and processes that are used to extract botanical oils, terpenoids, oleoresins and/or resins (generically referred to in this disclosure as “oils” or “plant oils”) from plant material or an oil containing substrate (generically referred to in this disclosure as “plant material”).
  • the method of extraction includes contacting the plant material with a heated gas and/or heated surface of a specific temperature such that the oils contained within the plant material are caused to volatilize and leave the plant material in the form of a vapor.
  • the vapor is then condensed and collected using a collection solvent in a manner that preserves and protects the integrity of the oil constituents.
  • the collection solvent utilized in the system is preferably ethanol or a mixture of ethanol and water, however, water, chloroform or a number of other suitable organic or inorganic solvents may be utilized to attain the desired results.
  • a method of separating the captured plant oils from the collection solvent is included whereby a substantially purified plant oil extract can be obtained as a final product of the system.
  • a few of the many types of plant materials that may be processed using the present invention may include various forms of hemp or cannabis that may generally be classified as Cannabis sativa, Cannabis indica, Cannabis ruderalis , hybridized crosses of various species or families of cannabis, or a mixture of one or more types of cannabis and/or other plant material.
  • the preferred oils to be extracted may include the various chemical forms of cannabidiol (CBD), cannabidivarin (CBDV), delta-9-tetrahydrocannabinol (THC), delta-8-tetrahydrocannabinol, tetrahydrocannabivarin (THCV), cannabinol (CBN), cannabigerol, cannabichromene, chemically converted cannabinoids or any other cannabinoid.
  • CBD cannabidiol
  • CBD cannabidivarin
  • THC delta-9-tetrahydrocannabinol
  • THCV delta-8-tetrahydrocannabinol
  • THCV tetrahydrocannabivarin
  • CBN cannabinol
  • cannabigerol cannabichromene
  • any plant material may be processed by the present invention and any plant oils may be targeted as the oils to be extracted.
  • An embodiment of the present invention provides a system for extracting an oil from plant material.
  • a gas moving device is operable to propel a gas stream through the system, the gas stream being a stream of air or gas with or without entrained vapor, solids or droplets of liquid therein.
  • An extraction chamber is in communication with the gas moving device such that the gas stream is directed through the extraction chamber, the extraction chamber operable to volatize at least a portion of an oil from a plant material such that the volatilized oil is disposed in the gas stream as an extracted oil.
  • a collection chamber is in communication with the extraction chamber such that the gas stream flows through the collection chamber, the collection chamber having collection solvent operable to collect at least a portion of the extracted oil from the gas stream.
  • a liquid collector in fluid communication with the collection chamber for collecting at least a portion of the collection solvent and extracted oil.
  • Some versions include a heater disposed such that the gas stream flows through the heater and the gas stream is heated.
  • the heater may be operable to heat the gas stream to a temperature sufficient to cause volatilization of the oil to be extracted, with the extraction chamber being in communication with the heater such that the heated gas stream is directed through the receiving area, the extraction chamber operable to volatilize the portion of the oil by the heated gas stream volatilizing the portion of the oil as the heated gas stream flows through the extraction chamber.
  • the extraction chamber may include a volatilization chamber having an upwardly facing entry tube and an exit disposed below the entry tube such that the gas flow impacts an upper end of the volatilization chamber and reverses direction before exiting the volatilization chamber.
  • the extraction chamber may be a modified spray dryer having a nozzle, the heated gas stream with entrained plant material being introduced through the nozzle.
  • the heater is operable to heat the gas stream at an exit of the heater or in the extraction chamber to a temperature in the range of 290 to 430 degrees Fahrenheit. In certain examples, the heater is operable to heat the gas stream to a temperature of at least 290 degrees Fahrenheit.
  • the heater may be a tube-in-shell heat exchanger with a steam generator providing steam to the heat exchanger or is an electric heater.
  • the extraction chamber includes a volatilization chamber having at least one heated surface and the portion of the oil is volatilized by the plant material contacting the heated surface.
  • the at least one heated surface has a temperature is in the range of 290 to 430 degrees Fahrenheit. In some examples, the at least one heated surface has a temperature of at least 290 Fahrenheit.
  • the extraction chamber may have a tangential entrance.
  • the extraction chamber includes a flash drying volatilization chamber having an entrance and an exit, the exit being above the entrance such that the gas stream flows upwardly and entrained plant materials are carried upwardly by the gas stream.
  • the entrance may be a nozzle.
  • the extraction chamber comprises a volatilization chamber having a tangential entrance.
  • the extraction chamber includes elements to break up clumps of plant material.
  • elements to break up clumps of plant material include balls, beads and rotating elements.
  • the extraction chamber includes an insulated and/or heated shell.
  • the extraction chamber may include a plurality of volatilization chambers in series and/or parallel.
  • Some versions of the extraction chamber may have a receiving area for receiving plant material for extraction.
  • Certain embodiments further include a plant material entrainment zone in communication with the gas stream mover such that the gas stream flows through the plant material entrainment zone, the plant material entrainment zone forming at least a part of the extraction chamber.
  • a hopper for holding plant material and a plant material portioning device operable to introduce the plant material into the plant material entrainment zone may also be included. Examples of the plant material portioning devices include an auger screw, a rotary valve, and a rotary airlock valve.
  • the collection chamber has at least one collection solvent sprayer operable to spray droplets of collection solvent into the gas stream such that at least some of the extracted oil dissolves into the collection solvent droplets and at least some of the collection solvent droplets flow to the liquid collector.
  • the at least one collection solvent sprayer may be a plurality of collection solvent sprayers and the collection solvent droplets may generally have a diameter greater than one micron and less than 300 microns.
  • the collection chamber may have packing material disposed therein with the packing material wetted by the collection solvent.
  • the system includes a secondary liquid separator in communication with the collection chamber.
  • the system includes a cooling chamber in communication with the extraction chamber such that the heated gas stream flows through the cooling chamber, and the cooling chamber is operable to cool the heated gas stream to or below a volatilization temperature of the extracted oil such that at least some of the extracted oil liquefies into droplets entrained in the gas stream.
  • the collection chamber is downstream of the cooling chamber.
  • the cooling chamber may be a spray cooling chamber having a high pressure sprayer operable to spray collection solvent into the heated gas stream such that the collection solvent rapidly cools the heated gas stream to or below a condensation temperature of the oil.
  • the sprayed collection solvent may be collection solvent and extracted oil from the liquid collector, and the system may further include a pump operable to pump the collection solvent and extracted oil from the liquid collector to the high pressure sprayer. Alternatively, the sprayed collection solvent is a substantially purified collection solvent.
  • a collection solvent cooler may be provided to cool the collection solvent for the high pressure sprayer.
  • interior surfaces of the extraction chamber and portions of the system downstream of the extraction chamber and upstream of the collection and/or cooling chamber are maintained at a temperature sufficient to prevent condensation of the volatilized oils on said interior surfaces.
  • the temperature sufficient to prevent condensation is in the range of 290 to 430 degrees Fahrenheit.
  • Some embodiments include a gas stream cooler in communication with the extraction chamber.
  • the gas stream cooler may be a tube-in-shell heat exchanger.
  • Some embodiments include an agglomeration chamber in communication with the cooling chamber or extraction chamber so as to receive the gas stream, the agglomeration chamber increasing the droplet size in the gas stream.
  • the agglomeration chamber may have a diameter greater than a diameter of a passage upstream of the agglomeration chamber such that the gas stream slows down in the agglomeration chamber.
  • the agglomeration chamber may include at least one collection solvent vapor injector operable to introduce a collection solvent vapor to the agglomeration chamber.
  • the agglomeration chamber may have a flow of cool gas that mixes with the heated gas stream.
  • An oil/solvent separation system may be provided to generally separate the collection solvent from the extracted oil so as to provide a generally purified collection solvent and a generally purified oil, with the separation system providing collection solvent vapor to the at least one collection solvent vapor injector.
  • passages or chambers disposed downstream of the extraction chamber have inner surfaces with a temperature less than a condensation temperature of the collection solvent such that collection solvent vapor entrained in the gas stream condenses on the inner surfaces and forms a solvent liquid that washes accumulated oils and collection solvent containing dissolved oils from the inner surfaces, the combined liquid flowing to the liquid collector.
  • the temperature less than a condensation temperature is in the range of approximately 85 to 145 degrees Fahrenheit.
  • interior surfaces of the extraction chamber are heated to a temperature sufficient to prevent condensation of the volatilized oils on the interior surfaces.
  • Some embodiments include an oil/solvent separation system operable to generally separate the collection solvent from the extracted oil so as to provide a generally purified collection solvent and a generally purified oil.
  • the separation system may include an evaporation device, and may also include a condenser to condense solvent vapor from the evaporation device.
  • Some embodiments include a plant material separation device in communication with and downstream of the extraction chamber, the plant material separation device operable to separate at least a portion of the plant material entrained in the gas stream therefrom.
  • the plant material separation device may be a cyclone or centrifugal separator and/or the separator has a heated exit and/or the separator has a heated backflow to displace vapors.
  • the plant material separation device may also include a secondary entrainment zone and a secondary gas stream mover operable to propel a secondary gas stream through the secondary entrainment zone, the plant material separation device providing the separated portion of plant material to the secondary entrainment zone.
  • a secondary plant material separator may be in communication with the secondary entrainment zone.
  • the secondary gas stream has a temperature less than a temperature of the gas stream flowing through the plant material separation device.
  • a gas stream filter may be in communication with the plant material separation device.
  • Some embodiments include a collection solvent separation device for separating at least a portion of the collection solvent from the gas stream.
  • Certain embodiments include a gas pump operable to remove gas from the system so as to maintain an interior pressure below atmospheric and prevent outward leakage from the system.
  • the collection solvent is: a non-toxic, food-grade solvent; a mixture of ethyl alcohol and water; a mixture of organic ethyl alcohol and water; or a solvent containing at least 40% ethyl alcohol.
  • the collection solvent is ethanol, a mixture of ethanol and water, water, chloroform or organic or inorganic solvents.
  • At least a portion of the collection solvent and extracted oil is recirculated to the collection chamber.
  • the plant materials are raw plant portions or partially processed plant portions and the extracted oil includes terpenoids.
  • the system is a substantially closed loop system.
  • the liquid collector is a sump in fluid communication with at least the collection chamber.
  • the plant materials are raw plant portions or partially processed plant portions and the system is extracting one or more specific saps, resins, oleoresins, lipids, terpenoids or otherwise volatilizable constituents within a plant material that is being processed.
  • the gas stream includes a gas selected from air, inert gas, reducing gas and mixtures thereof.
  • the gas stream mover may be a blower.
  • the present invention also includes use of any apparatus described herein to provide an extracted oil.
  • the gas moving device is part of the collection chamber.
  • the heater and/or the plant material separator and/or the gas stream filter 49 and/or the extraction chamber are insulated and/or heated.
  • the present invention includes a method for extracting an oil from plant material. Any system described herein may be used.
  • a plant material is provided in the extraction chamber and oil is volatilized from the plant material, the oil being extracted into the gas stream.
  • the gas stream is contacted with a collection solvent such that at least some of the oil is captured by the collection solvent. At least a portion of the oil and collection solvent is collected from the gas stream.
  • the plant material is exposed to the heated gas stream, the gas stream being heated to a temperature sufficient to cause volatilization of an oil to be extracted from the plant material.
  • the contacting and collecting steps comprise flowing at least a portion of the gas stream through a collection chamber and spraying the at least a portion of the gas stream with collection solvent such that at least some of the oil in the gas stream is captured by the collection solvent and at least some of the collection solvent flows to the collection chamber.
  • the plant material is one or more types of cannabis.
  • the extracted oil contains one or more of: cannabidiol (CBD); cannabidivarin (CBDV); delta-9-tetrahydrocannabinol (THC); delta-8-tetrahydrocannabinol; tetrahydrocannabivarin (THCV); cannabinol (CBN); cannabigerol; cannabichromene; chemically converted cannabinoids; or other cannabinoids.
  • CBD cannabidiol
  • CBDDV cannabidivarin
  • THC delta-9-tetrahydrocannabinol
  • delta-8-tetrahydrocannabinol tetrahydrocannabivarin
  • THCV tetrahydrocannabivarin
  • CBN cannabinol
  • cannabigerol cannabichromene
  • chemically converted cannabinoids or other cannabinoids.
  • the extraction chamber is operated at a temperature of approximately 315 degrees Fahrenheit.
  • the extraction chamber is operated at a temperature of approximately 356 degrees Fahrenheit.
  • the extraction chamber is operated at a temperature of approximately 428 degrees Fahrenheit.
  • FIG. 1 is a diagrammatic view of an embodiment of the present invention
  • FIG. 2 is a diagrammatic view of an alternative embodiment of the present invention.
  • FIG. 3 illustrates an embodiment of a volatilization chamber designed to expose plant material entrained in the primary gas stream to a highly-turbulent and highly-agitatative environment to facilitate rapid volatilization of plant oils contained within the plant material;
  • FIG. 4 illustrates an embodiment of the volatilization chamber that is also designed to expose the plant material entrained in the primary gas stream to a highly-turbulent and highly-agitatative environment to facilitate rapid volatilization of the plant oils contained within the plant material;
  • FIG. 5 illustrates an embodiment of the volatilization chamber that is designed to centrifugally force the plant material into contact with the heated walls of the volatilization chamber to induce rapid volatilization of the plant oils;
  • FIG. 6 illustrates an embodiment of the volatilization chamber that utilizes a modified form of pneumatic flash drying to induce rapid volatilization of oils within the plant material
  • FIG. 7 illustrates an embodiment of the volatilization chamber that is designed to prevent plant material that is still heavily laden with oils or has clumped together from escaping the volatilization chamber until it has been broken up into small particles and fully stripped of its desirable oils;
  • FIGS. 8 a and 8 b illustrate a cross-sectional and a top view of an additional embodiment of the volatilization chamber that is designed to prevent plant material that is still heavily laden with oils or has clumped together from escaping the volatilization chamber until it has been broken up into small particles and fully stripped of its desirable oils;
  • FIG. 9 is a detailed view of a primary plant material separation device and a secondary plant material entrainment section, for use with some embodiments.
  • FIG. 10 illustrates an embodiment that utilizes a collection chamber containing wetted packing.
  • FIG. 11 illustrates a simplified embodiment that uses little or no solvent.
  • FIG. 12 a illustrates an additional embodiment that uses little or no solvent and utilizes a centrifugal oil droplet separator.
  • FIG. 12 b illustrates an embodiment that uses little or no solvent and utilizes a centrifugal blower as a centrifugal oil droplet separator.
  • FIG. 13 illustrates an embodiment that uses little or no solvent and also facilitates continuous fractionation of the plant oils being extracted.
  • FIG. 14 illustrates an embodiment that uses little or no solvent, facilitates continuous fractionation of the plant oils being extracted and utilizes a centrifugal oil droplet separator.
  • FIG. 15 illustrates an embodiment that uses little or no solvent, facilitates continuous fractionation of the plant oils being extracted and utilizes a centrifugal gas mover as an oil droplet separator.
  • FIG. 16 illustrates an embodiment that uses little or no solvent and utilizes electrostatic collection plates to facilitate removal of plant oils from the gas stream.
  • FIG. 17 illustrates an embodiment that uses little or no solvent and utilizes demisting pads and/or packing material to facilitate removal of plant oils from the gas stream.
  • FIG. 1 illustrates a diagrammatic view of the primary system parts of an embodiment of the present invention.
  • a system is provided that includes a substantially closed network of passages and chambers containing a moving primary gas stream 1 (generically referred to in this disclosure as the “primary gas stream” or “primary gas flow”), a primary gas stream heater 2 , a steam generator 3 to provide a heat source to the primary gas stream heater 2 , a plant material or oil containing substrate hopper 4 , a plant material portioning device 5 , a primary plant material entrainment zone 6 , a plant material volatilization chamber 7 , a primary plant material separation device 8 , an optionally heated separated plant material exit 44 , a gas stream filter 49 , a cooling and condensation section 9 for contacting the primary gas stream with a cooling collection solvent spray 10 , a solvent spray cooler 11 , a gas stream cooler 50 , a primary pump 12 to provide pressurized collection solvent to various parts of the system, a sump area 13 to store collection solvent and
  • the primary gas stream 1 is propelled through the system by the primary gas stream mover 19 .
  • the primary gas stream may consist of atmospheric air, an inert gas such as but not limited to nitrogen, a reducing gas such as but not limited to CO2 or any other suitable gas or mixture.
  • the primary gas stream mover 19 is preferably a regenerative blower, turbo blower, pressure blower or other form of centrifugal blower, however, the primary gas stream mover may consist of any mechanism or method capable of moving a gas.
  • the gas stream may be kept above, below or equal to atmospheric pressure as required for different applications or effects. As the primary gas stream moves through the system, it passes through the primary gas stream heater 2 .
  • the primary gas stream heater is preferably a tube-in-shell heat exchanger that receives its heat in the form of saturated steam of a specific pressure and temperature provided by a steam generator 3 system, however, dry steam, a heated gas or other forms of heat exchange may be used, including but not limited to utilizing a hot oil or thermal fluid system whereby a heated fluid is pumped through the heat exchanger. Other forms of steam, gas or fluid powered heat exchangers may also be used as the application requires.
  • the primary gas stream heater may use electric heating elements of various designs to heat the gas stream, including, but not limited to, star-wound heating coil designs. As the primary gas stream passes through the primary gas stream heater 2 , the primary gas stream is heated to a temperature that is suitable to volatize one or more of the plant oil constituents present in the plant material.
  • the primary gas stream 1 passes through a primary plant material entrainment section 6 of the system.
  • the plant material supply is located in a hopper section 4 of the system.
  • a portioned amount of plant material is introduced to the primary plant material entrainment section 6 via an auger screw, a rotary valve, a rotary airlock valve or any other suitable distribution mechanism 5 .
  • the plant material is preferably introduced to the system in a finely shredded or powdered form, however, other consistencies may also be used depending on what is most preferable in different applications.
  • the plant material may be ground to the ideal or suitable consistency externally, or an integral grinder may be incorporated into the hopper 4 , portioning device 5 or entrainment section 6 system as described in, but not in any way limited by, PCT/IB2014/002383.
  • a few of the many types of plant materials that may be processed using the present invention may include various forms of hemp or cannabis that may generally be classified as Cannabis sativa, Cannabis indica, Cannabis ruderalis , hybridized crosses of various species or families of cannabis, or a mixture of one or more types of cannabis and/or other plant material. It should be noted that any plant material may be processed by the present invention and any plant oils may be targeted as the oils to be extracted.
  • the plant material becomes entrained in the heated primary gas stream 1 .
  • the entrained plant material travels with the primary gas stream into one or more volatilization chambers 7 placed in series or in parallel.
  • the primary entrainment zone and the volatilization chamber/chambers may together define an extraction chamber and, in some embodiments, may be integrated with one another.
  • a preferred way to volatilize the plant materials may be to use a form of pneumatic flash drying, however, adaptations of spray drying, spin drying, pneumatic ring drying, spin dryers with agitators, dryers with classifiers, dryers with agitators, bed drying, any of the volatilization methods proposed in the figures or text of this disclosure or any other method suitable to volatilize the plant materials may be used.
  • Each of these methods will be known to those who are skilled in the art of drying food products, pharmaceutical products and industrial materials, however, the way that this invention is using these methods is unique.
  • FIGS. 3, 4, 5, 6, 7, 8 a and 8 b A detailed view of several embodiments of the volatilization chamber 7 is illustrated in FIGS. 3, 4, 5, 6, 7, 8 a and 8 b , and will be discussed in greater detail in the following sections of this disclosure.
  • the plant material is agitated and circulated while being exposed to the heated primary gas stream to cause rapid volatilization of particular plant oils that volatilize near, at or below the temperature maintained within the volatilization chamber by the primary gas stream.
  • the plant material is forced into contact with a heated surface within the volatilization chamber.
  • the temperature of the gas stream exiting the heater 2 may be adjusted to maintain a desired temperature in the volatilization chamber/s and to counteract any temperature losses as the gas stream travels from the heater 2 to the volatilization chamber/s 7 .
  • targeting a specific temperature within the volatilization chamber will volatilize plant oil compounds that volatilize near or below such a temperature.
  • a method of successively processing the plant material at increasing temperatures over multiple extraction cycles may be used to fractionally isolate specific oils or specific groups of oils.
  • a sufficiently high temperature may be selected to volatilize a range of targeted plant oils in a single extraction cycle. Such methods will be well understood by those of skill in the art.
  • the preferred oils to be volatilized may include the various chemical forms of cannabidiol (CBD), cannabidivarin (CBDV), delta-9-tetrahydrocannabinol (THC), delta-8-tetrahydrocannabinol, tetrahydrocannabivarin (THCV), cannabinol (CBN), cannabigerol, cannabichromene, chemically converted cannabinoids or any other cannabinoid.
  • CBD cannabidiol
  • CBD cannabidivarin
  • THC delta-9-tetrahydrocannabinol
  • THCV delta-8-tetrahydrocannabinol
  • THCV tetrahydrocannabivarin
  • CBN cannabinol
  • cannabigerol cannabichromene
  • chemically converted cannabinoids or any other cannabinoid any other cannabinoid.
  • linalool linalool
  • caryophyllene myrcene
  • limonene limonene
  • humulene humulene
  • pinene By manipulating the temperature of the gas stream and/or heated surfaces that contact the plant materials within the volatilization chamber and completing successive extraction cycles, it is possible to isolate the various plant oils into substantially purified fractions. Alternatively, it is possible utilize a wider temperature band within the volatilization chamber to extract a range of plant oils in a single extraction cycle.
  • volatilization chamber temperatures may be utilized to extract various types of oils from cannabis:
  • the temperature within the volatilization chamber should be kept near 315 degrees Fahrenheit.
  • the temperature should be kept near 315 degrees Fahrenheit in the first extraction cycle to first remove the delta-9-tetrahydrocannabinol from the plant material, and then the plant material should be processed a second time at a temperature near 356 degrees Fahrenheit to remove the remaining cannabidiol.
  • the temperature within the volatilization chamber should be kept near 356 degrees Fahrenheit to volatilize both delta-9-tetrahydrocannabinol and cannabidiol in the same cycle.
  • the temperature of the volatilization chamber should be kept near 428 degrees Fahrenheit. Other combinations of different temperatures or successive extraction cycles may be used to target other oil compounds. Further discussion of temperatures and temperature ranges can be found in following sections of this disclosure.
  • the processed plant material and the volatilized plant oils may travel with the primary gas stream into a primary plant material separator 8 .
  • the oil may be referred to as an extracted oil.
  • a detailed view of an embodiment of the primary plant material separator 8 is illustrated in FIG. 9 and will be discussed in greater detail in a following section of this disclosure.
  • the processed plant material separator 8 is preferably a cyclone or centrifugal separator, however other centrifugal or non-centrifugal separation methods may be used to achieve the same or similar results.
  • the primary plant material separator 8 separates the processed plant material from the primary gas stream containing the volatilized plant oils.
  • the separated plant material exits through the bottom of the primary plant material separator, while the primary gas stream, along with the volatilized oils, exits through the top of the primary separator substantially free of entrained plant material. It should be noted that the positioning of the separated plant material exits and primary gas stream exits may be flipped or vary in placement depending on the differing requirements of the primary plant material separator design. Altering the placement of the exits should not be interpreted as being outside the scope of this invention.
  • the separated processed plant material exiting the primary plant material separator 8 may optionally become entrained in a secondary gas stream 25 in a secondary entrainment zone 27 , or may simply be in communication with a collection bin 29 .
  • the secondary gas stream 25 is propelled by a secondary gas stream mover 26 , which is preferably a centrifugal blower. However, any other method of propelling the secondary gas stream may be used.
  • the secondary gas stream is preferably kept at a lower temperature than the volatilization temperature of the plant oils in order to cool the processed plant material and prevent any continued volatilization or scorching from occurring.
  • the processed plant material travels with the secondary gas stream into a secondary plant material separator 28 .
  • the secondary separator 28 which is preferably but not limited to a cyclone or centrifugal separator, separates the processed plant material from the secondary gas stream. However, any method capable of separating some or all of the processed plant material may be used.
  • the processed plant material exits through the bottom of the secondary separator and is collected in a processed plant material collection bin 29 .
  • the secondary gas stream exits through the top of the secondary separator 28 substantially free of entrained plant material and continues to recirculate through the secondary gas stream loop 25 .
  • Other forms of plant material separation and collection may be used, such as the methods commonly employed in shop vacuum cleaners.
  • a simple method of allowing the processed plant material to drop as a result of gravity or be mechanically propelled with an auger screw or other mechanical device from the bottom of the primary plant material separator 8 into a bin or disposal area may be used to avoid the need for a secondary gas stream 25 and the parts required for a secondary gas stream system. If such an alternative is used, it may be preferable in some applications to provide an airlock valve, flapper valve or other method of isolating the primary plant material separator from the outside atmosphere.
  • One possible method of placing the primary plant material separator 8 is illustrated in FIG. 2 , however, other methods may also be used.
  • the primary gas stream 1 and volatilized oils that exit the top of the primary separator 8 may optionally pass through a gas stream filter 49 .
  • the gas stream filter 49 is preferably designed to remove any or most of the remaining fine particulates from the gas stream that are not captured by the primary plant material separator.
  • the gas stream filter 49 is preferably constructed of suitable materials to withstand the temperature of the heated gas stream. Such materials may include, but are not limited to, fiberglass filters or strainers, stainless steel or metal filters or strainers, sintered metal or glass filters, ceramic filters, or filters constructed of any other suitable materials.
  • the primary gas stream 1 and entrained volatilized oils travel into a cooling chamber 9 , which may take the form of a cooling spray section 9 , as shown.
  • the primary gas stream and entrained volatilized oils may travel into the cooling spray section 9 after exiting the primary plant material separator 8 .
  • the primary gas stream 1 and entrained volatilized oils are contacted with a cooling spray 10 of a collection solvent that is emitted from one or more sprayers.
  • the cooling spray 10 is supplied by a primary pump 12 that moves collection solvent to various sprayers and other areas throughout the system. As illustrated in FIG.
  • the primary pump 13 draws collection solvent from the sump area 13 , however, in other embodiments, the primary pump 12 may draw collection solvent from other areas or other solvent reservoirs.
  • the cooling spray instead be supplied by a dedicated pump that draws from a reservoir or other source of substantially purified collection solvent.
  • FIG. 2 An example of such an embodiment is illustrated in FIG. 2 and a further description of such an embodiment is included in the sections of this disclosure that discuss the evaporation device 31 .
  • the collection solvent may be optionally cooled by a collection solvent cooler 11 .
  • the collection solvent cooler 11 may be placed within the system such that it only cools the collection solvent before reaching the cooling spray section 9 or it may be placed before or after the primary pump 12 such that collection solvent spray traveling to any parts of the system are cooled.
  • the collection solvent cooler 11 is preferably designed as liquid-cooled tube-in-shell heat exchanger or plate heat exchanger, however, air-cooled designs or any other suitable heat exchange device may be utilized.
  • the collection solvent cooler 11 may be cooled by any type of fluid or gas.
  • the cooling supply may be a liquid or gas that is pumped through an air-cooled or liquid-cooled heat exchange device, a municipal water supply or any other suitable method.
  • providing sufficient cooling to the collection solvent system can provide cooling and temperature regulation of the entire system, in addition to that which is required to provide cooling to the cooling section 9 .
  • a further discussion of potential heat exchanger designs can be found in the sections of this document describing the gas stream cooler 50 and evaporation device 31 condenser.
  • the designs and cooling methods used for the collection solvent cooler 11 , gas stream cooler 50 , the solvent recovery device 22 and evaporation device 31 condenser may be used interchangeably as needed for each cooler or condenser device to function as required in different embodiments and applications.
  • the primary gas stream Upon being contacted with the cooling spray 10 within the cooling spray section 9 , the primary gas stream is cooled and the volatized oils within the primary gas stream begins to condense.
  • the system and the flow rates of the gas stream and cooling spray solvent are designed such that a large portion of the volatilized oils condense directly on the surface of the cooling spray droplets, where they become directly captured in the collection solvent and drain directly or through other components of the system to reach the sump area 13 of the system.
  • Much or all of the oils that do not condense on the droplets condense within the gas stream into a fog of small and microscopic oil droplets, which travel out of the cooling section 9 entrained in the primary gas stream 1 .
  • a cooling spray 10 as a gas stream cooling and oil vapor condensation method
  • other methods including but not limited to contacting the primary gas stream with cooling coils, passing the primary gas stream through a tube-in-shell heat exchanger, or introducing a cooling gas directly into the primary gas stream.
  • element 10 may represent any of these components or more than one such component.
  • the primary gas stream may optionally pass through a gas stream cooler 50 .
  • the gas stream cooler 50 cools the gas stream, the entrained oil droplets and the mixture of collection solvent and captured plant oils preferably to a temperature that is sufficient to prevent heat degradation of the plant oils.
  • the gas stream cooler 50 is preferably designed as a tube-in-shell heat exchanger that uses a flow of liquid or gas as a coolant medium.
  • any air or liquid-cooled device may be used, including but not limited to exposing the gas stream to contact with vapor compression or absorption chiller coils.
  • any coolant may be used, including but not limited to municipal water, water or various types of coolant fluids pumped or moved with the aid of a pump, vapor compression or absorption chiller coils or any other suitable method.
  • the liquid coolant may be cooled using forced air, passive air, a vapor compression or absorption chiller, heat exchange with another liquid or any other suitable method.
  • the gas stream cooler 50 may be cooled with forced air that is moved by the aid of an air mover, cool air from a vapor compression or absorption chiller, evaporative cooling from a swamp cooler or similar device or by passive contact with the surrounding atmosphere. It should be noted that providing sufficient cooling to the gas stream cooler 50 can provide cooling and temperature regulation of the entire system.
  • gas stream cooler be placed directly after a cooling spray 10 or collection solvent spray section such that the collection solvent washes any condensed oils from the gas stream cooler 50 and such that the time that the collection solvent and plant oils are exposed to heat is minimized, however, other placements may be used.
  • the primary gas stream containing a fog of any entrained oil droplets that were not previously captured by the cooling spray enters a sump section/liquid separator 13 .
  • the primary gas stream and entrained oil droplets may enter the sump section 13 after exiting the cooling spray section 9 .
  • the sump section 13 separates the majority of the liquefied collection solvent and extracted plant oil mixture from the primary gas stream and serves as a holding area for the collection solvent and captured extracted plant oil.
  • Such a separate liquid separator could be as simple as a tee or bend in the gas stream path or may include demisting pads or other more advanced methods of separation.
  • a separate collection solvent reservoir (not shown) containing substantially purified collection solvent may also be included as a method to replenish any collection solvent that is lost or removed from the system as it operates.
  • the primary gas stream and the fog of entrained oil droplets optionally enter an agglomeration section 14 .
  • the diameter of the agglomeration section 14 is preferably larger than that of the other passages within the primary gas stream loop 1 or is otherwise designed to be large enough to lower the velocity of the primary gas stream and maximize the time that the primary gas stream and the fog of oil droplets remain within the agglomeration section 14 . It is also possible to use a longer agglomeration section, adjust the gas stream velocity, or use multiple agglomeration sections in parallel or in series to attain a similar result of maximizing the time that the oil droplets spend in the agglomeration section.
  • the gas stream and fog of oil droplets are contacted with collection solvent vapor provided by collection solvent injectors 15 .
  • the collection solvent vapor 15 condenses on the surface of the cooler oil droplets, causing them to grow larger and increase in size and mass. Increasing the size and mass of the entrained oil droplets greatly enhances their removal from the gas stream in subsequent sections of the system.
  • the preferred source of the collection solvent vapor is from the distilled collection solvent outlet of the evaporation device 31 , however, other methods of providing collection solvent vapor may be used.
  • mixing a cooler gas stream with a warmer gas stream as it enters the agglomeration section will achieve a similar result. Such an alternative method is described in PCT/IB2014/002383.
  • the diameter of the entrance of the agglomeration section and the passages leading from the sump area 13 to the agglomeration section 14 should be designed to be large enough to reduce the velocity of the primary gas stream such that condensing liquids can easily drain against the flow of the primary gas stream to reach the sump area 13 .
  • this may not be a requirement in some applications or with certain positionings of the agglomeration chamber within the system, such as when the gas stream enters through the top of the agglomeration section and exits through the bottom, for example.
  • the primary gas stream 1 and mist of enlarged oil droplets enter a collection chamber section 16 .
  • the primary gas stream and entrained oil droplets may enter the collection chamber section 16 after leaving the sump section 13 .
  • the oil droplets entrained in the primary gas stream are bombarded with a high pressure spray 17 of collection solvent droplets emitted from one or more collection solvent sprayers 17 . Any oil droplets that are impacted with collection solvent droplets 17 are effectively captured in the collection solvent, which collides with the walls of the collection chamber 16 and eventually drains to the sump area 13 .
  • the collection chamber section 16 could be considered to be the cooling section 9 and the cooling 9 section could be considered to be the collection chamber 16 section.
  • the function of both the cooling spray section and the collection chamber section could be combined into one section in some embodiments of the system.
  • the combined cooling spray/collection chamber section be located directly after the primary plant material separator 8 or directly after the gas stream filter 49 , and in front of the gas stream cooler 50 .
  • the cooling section may be considered to be the gas stream cooler 50 or another cooling device or cooling area.
  • the primary gas stream optionally travels onward through a secondary liquid separation section 18 .
  • the secondary liquid separation section 18 separates the majority of the collection solvent from the primary gas stream to prevent the primary gas stream mover 19 from being overwhelmed by collection solvent.
  • the secondary liquid separation section 18 may be as simple as a tee or bend in the gas stream passage or may include more advanced separation methods.
  • the separated collection solvent drains from the liquid separation section 18 and back into the sump section 13 of the system.
  • the liquid separation section 18 may not be needed, depending on the ability of the primary gas stream mover 19 to handle entrained liquids. In other embodiments, it may be desirable to intentionally introduce some liquid into the gas stream mover 19 to facilitate cleaning and/or cooling of the gas stream mover 19 .
  • the primary gas stream exiting the liquid separation section 18 enters the primary gas stream mover 19 .
  • the primary gas stream enters the primary gas stream mover 19 after leaving the collection chamber 16 .
  • the primary gas stream mover 19 is preferably a regenerative blower, turbo blower, pressure blower or another type of blower that subjects the gas stream to a high level of centrifugal force, however, any method of propelling the primary gas stream may be used.
  • the primary gas stream Upon entering the primary gas stream mover 19 , the primary gas stream is subjected to high centrifugal forces.
  • the gas stream mover may be utilized as the primary method of separating the entrained plant oil droplets from the gas stream.
  • the gas stream mover be supplied with a spray or stream of collection solvent to facilitate in washing the captured plant oils from the blower blades and housing.
  • the gas stream mover or gas moving device may be considered part of the collection chamber and/or the gas moving device may form the only collection chamber for certain versions.
  • the arrangement of the gas stream mover within the system may also be altered depending on the embodiment and application.
  • the primary gas stream exiting the primary gas stream mover 19 travels into an optional droplet separator 20 .
  • This droplet separator 20 is preferably a cyclone or centrifugal separator, although other methods may be used. The droplet separator separates much or all of the remaining liquid droplets from the primary gas stream. The separated collection solvent and oil drains from the separator 20 into the sump area 13 of the system.
  • an optional positive displacement/airlock pump 33 or similar device may be used to facilitate the drainage of the droplet separator 20 to the sump section 13 of the system.
  • Such an airlock/pump 33 or similar device may also be used in embodiments that do not include an optional droplet separator 20 to facilitate drainage directly from the primary gas stream mover 19 .
  • An airlock/pump 33 or similar device may also be used for a similar function in embodiments that include the optional demister/polishing section 21 described in the following paragraph.
  • the primary gas stream After exiting the droplet separator 20 , the primary gas stream optionally enters a demister/polishing section 21 .
  • the primary gas stream may enter the demister/polishing section 21 after exiting the gas stream mover 19 .
  • the polishing section 21 polishes the primary gas stream and serves as a final droplet separation stage to remove much or all of the remaining collection solvent droplets prior to the primary gas stream passing through the primary gas heater. Providing effective droplet separation in the polishing section 21 and/or any preceding droplet separation sections prevents any droplets containing plant oils from coming in contact with the heated sections of the primary gas stream heater 2 , thus preventing plant oils from burning, fouling or breaking down on the hot heater surfaces.
  • some embodiments provide a method of connecting the closed portion of the system to the atmosphere. Connection to the atmosphere is established through a solvent recovery device 22 such that as gases pass out of the system, any evaporated collection solvent is condensed and returned to the system.
  • the solvent recovery device 22 is preferred to prevent collection solvent or volatilized plant oils from entering the surrounding atmosphere.
  • the solvent recovery device 22 may utilize any known method of solvent recovery, including but not limited to a cold trap, a condensation tube, a filter, a distillation column, a commercially available solvent recovery system or any other suitable method.
  • the solvent recovery device 22 may also contain a carbon filter or other type of odor capturing filter to prevent odors from escaping the system.
  • Various condenser designs may be employed as the solvent recovery device 22 , including any of the condenser designs discussed below in the paragraphs describing the evaporation device condenser 55 .
  • An optional out-only check valve 23 is attached to the exit end of the solvent recovery device 22 to allow expanding gases to escape from the system when the system is heating and to prevent any atmospheric gases from traveling backwards into the system through the solvent recovery device 22 when the system is cooling.
  • an in-only check valve 30 may be connected to the processed plant material collection bin 29 or other places within the system.
  • collection solvent vapors be evacuated from this portion of the system to prevent their escape into the surrounding atmosphere.
  • an evacuation pump 24 may be attached to the exit of the solvent recovery device 22 .
  • An additional benefit of using an evacuation pump 24 in this manner is that the potential for solvent vapors escaping through any leaky seals within the system is mitigated.
  • a displacing gas may be introduced to the processed plant material bin or any other areas within the system that are deemed desirable to displace.
  • a preferred displacing gas would be CO2 or nitrogen, however, other displacing gases may be used. It should be known that utilizing an evacuation pump 24 or displacing gas is beneficial for multiple purposes (including preventing the condensation of volatilized oils at the plant material exit of the primary plant material separation device 8 ) and such use is not in any way dependent on a need to evacuate the processed plant material collection bin 29 .
  • the evacuation pump 24 and/or addition of a displacing gas creates a slight backflow through the plant material separator 8 and serves an important function to prevent volatilized plant oils from escaping from the separated plant material exit 44 of the primary plant material separator 8 and condensing on the separated plant material exit 44 of the primary plant material separator 8 and/or the parts within the secondary gas flow loop 25 and/or processed plant material bin 29 . If plant oils condense in these areas, it could cause plant material to stick to the internal surfaces of these parts and block the flow of separated plant material to the collection bin 29 . While a passive method of evacuating plant oil vapors from these areas to prevent condensation is preferred, in some embodiments, it may be beneficial to include an auger screw or mechanical scraping method to ensure that these parts never become clogged.
  • some versions of the invention may optionally include an oil/solvent separation system such as an evaporation device 31 .
  • the evaporation device 31 is preferably, but not limited to, an evaporation device such as a thin film evaporator, wiped film evaporator, short path evaporator, rising film evaporator, falling film evaporator, spray dryer evaporator, centrifugal thin-film evaporator, or a conventional still design such as, but not limited to, stills that are commonly used to distill ethanol-based spirits.
  • any suitable evaporation device may be used and one or more evaporation devices may be used alone or in combination for enhanced evaporation or multiple effect evaporation.
  • Non-evaporative oil separation devices may alternatively be utilized.
  • the evaporation device 31 may be operated at atmospheric pressure, under vacuum or above atmospheric pressure. Heat may be supplied to the evaporation device using electric heating elements, steam from a steam generator, a hot oil system, a thermal fluid, a heated gas or any other suitable method of supplying heat.
  • the evaporation device is a thin film or wiped film evaporator
  • heat be supplied to the evaporator by wrapping the evaporation section with heat cables or by including a steam jacket or thermal fluid jacket around the evaporation section of the device and providing heat with a steam generator or thermal fluid system.
  • the evaporation device is a rising film or falling film evaporator
  • heat be supplied to the falling or rising film section by a steam generator or thermal fluid system.
  • the evaporation device 31 draws a portioned flow of the mixture of collection solvent and captured plant oils from the sump area of the system by diverting some of the pressurized solvent from the primary pump 12 with the aid of a proportional valve, solenoid valve or other suitable diversion and/or portioning method (not shown) or with the aid of a dedicated feed pump 60 (shown in FIG. 2 ).
  • the collection solvent is evaporated and distilled from the solvent and plant oil mixture and the solvent is reintroduced to the system as a substantially purified collection solvent.
  • the purified collection solvent is reintroduced to the system as a vapor via collection solvent vapor injectors 15 in the agglomeration section 14 of the system.
  • the evaporated collection solvent vapors may be used to facilitate the function of the agglomeration section 14 .
  • the purified collection solvent may additionally or alternatively be introduced as a vapor to other sections of the system to aid in cleaning of the various components or serve other functions as required.
  • the plant oils which preferably have a higher boiling point than the collection solvent utilized, do not readily evaporate within the evaporation device 31 and are concentrated into a substantially pure form as the collection solvent is distilled away.
  • the concentrated plant oils exit the evaporation device 31 as a substantially pure extract which is subsequently collected in an extract collection area 32 as a final product of the system. Additional discussion of evaporation methods can be found in PCT/IB2014/002383, however, these methods should not be viewed as limiting.
  • other methods of separating the plant oils from the collection solvent may be used.
  • stratification methods of separation may be employed. Chromatography methods may also be used to separate the oils from the collection solvent. Such methods serve as examples and are not limiting. Those of skill in the art will be able to determine the best separation method for different applications of the current invention.
  • FIG. 2 illustrates an additional embodiment of the present invention.
  • the substantially purified collection solvent vapor exiting the evaporation device 31 passes through a condenser 55 to condense the collection solvent vapor into a liquid.
  • the liquefied collection solvent exiting the condenser 55 flows into a purified solvent reservoir 56 .
  • a dedicated collection solvent pump 57 draws the substantially purified collection solvent from the purified solvent reservoir 56 and sprays the purified collection solvent directly into the cooling spray section 9 via the cooling spray 10 .
  • the purified solvent may be pumped directly from the condenser 55 .
  • any condenser design may be used, including but not limited to liquid-cooled designs such as a Liebig, Allihn, Graham, Dimroth, Fridrichs or tube-in-shell condenser, or air cooled designs such as spiraled tubes, radiator style condensers or other designs that will be readily known to those of skill in the art.
  • any coolant may be used, including but not limited to municipal water, water or various types of coolant fluids pumped or moved with the aid of a pump, vapor compression or absorption chiller coils or any other suitable method.
  • the liquid coolant may be cooled using forced air, passive air, a vapor compression or absorption chiller, heat exchange with another liquid or any other suitable method.
  • the condenser may be cooled with forced air that is moved by the aid of an air mover or by passive contact with the surrounding atmosphere.
  • Such condenser designs and cooling methods may also be employed in the solvent recovery device 22 , as mentioned above.
  • the gas stream heater 2 In order to maintain the temperature of the gas stream and to prevent condensation of volatilized oils on undesired surfaces within the heated portions of the system, in many embodiments of the invention it will be advantageous to house all or most of the heated portions of the system, including but not limited to all, some or any combination of the gas stream heater 2 , the primary plant material separator 8 , the primary plant material separator lower exit 44 (discussed in further detail in a following section), the optional gas stream filter 49 and the volatilization chamber/s 7 , together in one passively insulated or actively heated box or heated chamber to simplify the insulating or heating of such components.
  • Such a heated chamber may be passively insulated with a thermal insulation barrier such as fiberglass, ceramic wool, silica insulation, calcium silicate, aerogel, ceramic insulation, rock wool, mineral wool or any other suitable insulating medium.
  • a thermal insulation barrier such as fiberglass, ceramic wool, silica insulation, calcium silicate, aerogel, ceramic insulation, rock wool, mineral wool or any other suitable insulating medium.
  • electric elements may be used within the open space of the oven cavity with or without the aid of a convection fan, or a heated gas may be pumped through the oven chamber.
  • the heated parts may be housed together in a vacuum chamber of suitable size for passive insulation, or a steam chamber of suitable size that may be supplied with steam as a heat source for active heating.
  • the heated parts may also be wrapped with a heating cable.
  • the heated parts may be contained in a chamber with a thermal heating liquid.
  • any heating or insulating method known to those of skill in the art may be utilized and still fall within the scope of this invention. It should be known that in most embodiments it may be important to construct the gas stream path such that the hopper section 4 is not housed within the oven chamber, yet is able to provide plant material to the entrainment zone 6 . In embodiments wherein the heated components of the system are not contained within a heated box/oven chamber, or in embodiments wherein additional heating or insulation of the heated components is required, the heated components may be individually insulated or actively heated as discussed in the following sections of this document.
  • a method of cooling the overall system must be used to prevent the system from overheating.
  • Various methods of cooling the overall system using the collection solvent cooler 11 and/or the gas stream cooler 50 have been discussed in this disclosure. Additional methods, such as, but not limited to, circulating forced air or a cooling fluid over the external parts of the system may also be used. Passive methods of cooling the system, such as, but not limited to, including cooling fins or protrusions on various components of the system and gas stream loop may also be employed. It is also possible to house the system in a room or chamber of a regulated temperature. Further discussion of various additional cooling methods can be found in PCT/IB2014/002383.
  • the gas stream in most embodiments of the present invention will be saturated with collection solvent vapors in some areas, it is possible to promote an environment in the cool sections of the system that causes collection solvent vapors to condense on the internal surfaces of these sections.
  • the condensing collection solvent can be used to aid in washing these surfaces of any accumulated plant oils.
  • the various valves, pumps, airlocks, electrical heaters and/or steam heaters, and any other controllable components of the system described in this disclosure may be regulated or controlled by mechanical methods and/or electronic temperature and/or pressure switches. It is, however, preferred that the temperatures and pressures within the system, the optional steam generator, evaporation device and various pumps, valves, airlocks, gas movers and other controllable components within the system be controlled by one or more programmable logic controllers (PLC control) and/or proportional integral derivative controllers (PID control) and/or other forms of computerized controls. Utilization of such electronic devices may achieve more precise control of the temperatures, pressures and various actions of the system.
  • PLC control programmable logic controllers
  • PID control proportional integral derivative controllers
  • the temperatures may be monitored by thermocouples, resistance temperature detectors (RTD sensors) and/or other temperature detection methods
  • the pressures may be monitored by electronic pressure sensors and/or mechanical pressure devices and/or other detection methods
  • the gas flow and liquid flow may be detected by electronic mass flow meters, pressure sensors, pressure differential sensors, Coriolis meters and/or other detection methods
  • the position of components may be detected with limit switches, position sensors, proximity sensors and/or other detection methods
  • the levels of fluids may be detected with optical, electrical, conductive, ultrasonic, capacitive, float switches and/or other detection methods
  • the levels of dry materials may be detected with optical, electrical, conductive, ultrasonic, capacitive, float switches, rotary dry level detectors and/or other detection methods.
  • sensors that can detect the saturation levels of water, plant oils or other liquids that have accumulated in the collection solvent mixture, such as capacitance sensors, conductivity sensors, specific gravity sensors, moisture sensors, refractometers or other types of sensors.
  • Other sensors of various available designs may also be utilized as needed to measure the state of the various components and still fall within the scope of this invention.
  • Non-limiting examples of how such thermocouples, sensors and devices that may be placed within the present invention can be found in PCT/IB2014/002383, which is incorporated in this application in its entirety by reference, however, the placement of sensors will be apparent to those who are skilled in the art.
  • the various temperature, pressure, flow rate and other sensors may be placed within any section of the system, in any quantity and in any order and still fall within the scope of this invention.
  • the various PLC, PID, computer or other control methods may regulate components within the system with various types of commercially available digital, analog and/or other types of input/output modules (IO modules), stepper controllers, variable frequency controllers, solid state relays, conventional magnetic relays and/or any other suitable method.
  • IO modules input/output modules
  • stepper controllers stepper controllers
  • variable frequency controllers solid state relays
  • solid state relays solid state relays
  • conventional magnetic relays conventional magnetic relays and/or any other suitable method.
  • FIG. 3 provides a detailed view of an embodiment of the volatilization chamber section of the system.
  • the purpose of the volatilization chamber is to expose the plant material entrained in the primary gas stream to a turbulent and/or agitated environment to maximize contact with the gas stream and facilitate rapid volatilization of the plant oils contained within the plant material.
  • This disclosure describes multiple methods to attain these results, including omission of the volatilization chamber in favor of a primary plant material separator with heated walls, however, other methods may be used to attain similar results and still fall within the scope of this invention.
  • the primary gas stream carries the entrained plant material into the volatilization chamber through an upward facing entry tube 34 .
  • the entrained plant material Upon leaving the tip of the entry tube 34 , which may include a high-velocity nozzle tip in some applications, the entrained plant material is blasted upward toward the top of the volatilization chamber 7 . As the plant material travels upward, it is exposed to a turbulent reversal of the gas stream flow within the volatilization chamber. This action causes forceful agitation of the plant material and maximizes its contact with the heated primary gas stream to facilitate rapid volatilization of the plant oils contained within the plant material. The primary gas stream, along with the entrained plant material, exit the volatilization chamber through an exit passage 35 at the bottom of the chamber and travel onward to the primary plant material separator 8 .
  • One or more volatilization chambers of this type may be used in series or in parallel or in combination with other types of volatilization chambers. As such, element 7 in FIG. 1 and FIG. 2 may represent one or more volatilization chambers.
  • volatilization chamber In order to maintain a sufficient temperature of the gas stream as it passes through the volatilization chamber and to prevent condensation of volatilized oils on surfaces within the volatilization chamber, it is preferred that most embodiments of the volatilization chamber discussed within this disclosure be contained or wrapped in a thermal insulation barrier and/or be provided with an active heat source. Such a heat source or thermal barrier may optionally be eliminated if the volatilization chamber/s are housed together with all or some of the other heated sections of the system within an insulated or heated chamber as discussed above. As a non-limiting example that may be applied to any of the embodiments of the volatilization chamber discussed or referred to in this disclosure, in FIG. 3 , the volatilization chamber is illustrated housed within a heating jacket 36 .
  • a heated gas of a specific temperature or a heated thermal fluid of a specific temperature is pumped or otherwise introduced to the heating jacket through an entry passage 37 .
  • the steam and/or condensed steam, heated gas or thermal fluid circulates out of the heating jacket through an exit passage 38 .
  • the steam be supplied by the same steam generator that provides heat to the primary gas heater 2 .
  • an electrical heat source within the jacket space or an electrical heating wire wrapped directly around the volatilization chamber may also be used. Any of these methods may be used to heat any of the embodiments of the volatilization chamber discussed or otherwise referred to in this disclosure.
  • a thermal insulation barrier such as fiberglass, ceramic wool, silica insulation, calcium silicate, aerogel, ceramic insulation, rock wool, mineral wool or any other suitable insulating medium. It may also be preferred in some applications to house the volatilization chamber within a vacuum jacket. As a non-limiting example, such a vacuum jacket may look substantially similar to the heating jacket 36 illustrated in FIG. 3 , except there would be no entry 37 or exit passages 38 for a heating medium. Instead, of heating medium entry and exit passages, an evacuation passage would be included that may include a check valve or similar vacuum containment method. Alternatively, the vacuum jacket may be permanently sealed or welded closed to retain the vacuum. Any of these methods may be used to insulate any of the embodiments of the volatilization chambers discussed or otherwise referred to in this disclosure.
  • FIG. 4 illustrates an additional embodiment of the volatilization chamber section 7 of the system that utilizes a modified spray drying technique.
  • Conventional industrial spray drying techniques typically involve spraying a mostly liquid feed that contains some solids into a heated gas stream as it enters a drying chamber. Those of skill in the art will be familiar with the design of such spray drying chambers.
  • the liquids are evaporated and subsequently vented as waste, while the solids are collected as the final product.
  • the opposite final product is desired. Instead of the solids being desired, the liquid portion is desired as a final product.
  • the utilization of the spray drying technique is modified in this invention to handle a mostly dry feed instead of a mostly liquid feed.
  • powdered or finely-ground plant material (a solid that contains liquid oils) is introduced into a heated gas stream that enters a drying chamber/volatilization chamber.
  • This heated gas stream is the primary gas stream as defined in this invention.
  • the primary gas stream carries the entrained plant material into the volatilization chamber 7 through a downward facing entry tube 39 with a nozzle tip.
  • the primary gas stream and plant material rapidly exiting the nozzle facilitates a turbulent flow of the heated gas stream within the volatilization chamber and agitates the plant material to cause rapid volatilization of the oils contained within the plant material.
  • One or more chambers of this type may be used in series or in parallel or in combination with any other types of volatilization chambers. Utilization of different nozzle designs, the addition of pressurized and/or hot air at the nozzle site, modifications to the dimensions and diameter of the spray drying chamber and other changes may benefit volatilization of the plant material and/or prevent plant material from sticking to the walls of the chamber in similar ways that such modifications benefit conventional spray drying techniques. In some embodiments, it may be advantageous to introduce the plant material directly at the nozzle site versus upstream of the nozzle in the entrainment area 6 .
  • volatilization chamber in order to maintain the temperature of the gas stream and to prevent condensation of the volatilized oils on the surfaces within the volatilization chamber, it is preferred that the volatilization chamber be provided with its own heat source and/or a thermal insulation barrier. Examples of such heat sources and thermal barriers were discussed above, and may be applied to all embodiments of the vaporization chamber.
  • FIG. 5 illustrates a third embodiment of the volatilization chamber 7 that is designed to centrifugally force the plant material into contact with the heated walls of the volatilization chamber to induce rapid volatilization of the plant oils.
  • One or more chambers of this type may be used in series or in parallel or in combination with other types of volatilization chambers.
  • the primary gas stream 1 and the entrained plant material enter the volatilization chamber through a tangential entrance 40 at the upper end of the volatilization chamber 7 .
  • the entrained plant materials are centrifugally forced into contact with the outer walls 41 of the chamber, where they spiral around the walls 41 of the volatilization chamber multiple times before eventually reaching the bottom exit 35 of the volatilization chamber.
  • the walls 41 of the volatilization chamber be in contact with a heat source.
  • a thermal barrier may suffice. Examples of such heat sources and thermal barriers are discussed above, and may be applied to this embodiment and all other embodiments of the vaporization chamber.
  • FIG. 6 illustrates an embodiment of the volatilization chamber 7 that utilizes a modified form of pneumatic flash drying to induce rapid volatilization of oils within the plant material.
  • One or more chambers of this type may be used in series or in parallel or in combination with other types of volatilization chambers.
  • the primary gas stream containing entrained plant material enters the flash drying volatilization chamber 7 through a bottom entry passage 46 and carries the plant material upwards against gravity before exiting the chamber through an exit passage 47 .
  • the upper exit passage 47 may be relocated to the side of the chamber, however, it is preferred that the lower entry passage 46 remain at the lowermost point of the chamber 7 .
  • the diameter of the flash drying chamber and the flow rate of the primary gas stream must be carefully designed such that the heated gas flowing through the chamber is moving slightly faster than the natural freefall velocity of the plant material particles being processed. At this gas stream velocity, contact of the heated gas stream and plant particles is maximized, causing rapid volatilization of the plant oils.
  • the length of the flash drying volatilization chamber 7 may be adjusted to maximize volatilization, or may be repeated with several shorter chambers arranged in series.
  • the volatilization chamber in order to maintain the temperature of the gas stream and to prevent condensation of the volatilized oils on the surfaces within the volatilization chamber, it is preferred that the volatilization chamber be provided with its own heat source and/or a thermal insulation barrier. Examples of such heat sources and thermal barriers are discussed above, and may be applied to all embodiments of the vaporization chamber.
  • FIG. 7 illustrates an additional embodiment of the volatilization chamber that is designed to prevent plant material that is still heavy laden with oils or has clumped into lumps from escaping the volatilization chamber until it has been broken up into small particles and has been fully stripped of its desirable oils.
  • This special type of volatilization chamber is an adaptation of a flash drying chamber that is designed such that the diameter of the chamber and the gas stream flow volume create a gas velocity that only allows the smallest and most thoroughly oil-stripped particles of plant material, which are light enough to float upward in the gas stream, to exit the top of the chamber. Larger lumps or oil laden plant particles, which are too heavy to be carried up and out of the chamber, remain tumbling in an agitation zone until they are broken up and evaporated of their oils.
  • the gas stream carrying entrained plant material enters the volatilization chamber through a bottom passage 46 .
  • the diameter of the bottom passage is reduced to a small diameter before entering the chamber to form an air blade nozzle 47 .
  • the high velocity air from the nozzle 47 turbulently enters the volatilization chamber and helps forcefully break apart any lumps or chunks of plant material that are too heavy to travel upward in the chamber.
  • the lighter and smaller particles of plant material are quickly stripped of their desired oils and continue to travel upward with the gas stream to exit the chamber through an exit passage 48 .
  • a non-limiting example of such an element is represented by a ball 51 in FIG. 7 .
  • the balls or other milling objects will be thrown around within the chamber by the air nozzle 83 to facilitate breaking up of the plant material.
  • An excluder screen or other exclusion method may optionally be included to prevent a stray ball or milling object from escaping the volatilization chamber.
  • the fast moving gas stream entering the chamber may be used to power a turbine blade (not shown) to a high velocity.
  • the optional high velocity turbine blade may be used to break up any large particles of plant material moving around the bottom sections of the chamber.
  • Such a blade could also be rotated by an externally powered shaft that passes through a wall of the chamber or incoming gas passage, or by a magnetic coupling to avoid the need for a shaft seal and/or shaft penetration hole that could potentially leak.
  • the blade and milling object designs used in this embodiment of the vaporization chamber could be adapted for use in any of the vaporization chamber embodiments discussed in this disclosure. While the volatilization chamber illustrated in FIG. 7 is illustrated as having a concave bottom area, in other embodiments it may be desirable to utilize a conical bottom area to continuously funnel the falling heavier plant materials back into the air pick or blade area.
  • the volatilization chamber in order to maintain the temperature of the gas stream and to prevent condensation of the volatilized oils on the surfaces within the volatilization chamber, it is preferred that the volatilization chamber be provided with its own heat source and/or a thermal insulation barrier. Examples of such heat sources and thermal barriers are discussed above, and may be applied to all embodiments of the vaporization chamber.
  • FIGS. 8 a and 8 b illustrate a cross-sectional and a top view of another embodiment of the volatilization chamber that is designed to prevent plant material that is still heavy laden with oils or has clumped into lumps from escaping the volatilization chamber until it has been broken up into small particles and been fully stripped of its desirable oils.
  • the gas stream and entrained plant material enters the volatilization chamber through a tangential side entrance 70 .
  • the gas stream enters at a high velocity and causes the entrained plant materials to spiral rapidly within the volatilization chamber.
  • hollow or solid balls or beads or other milling objects of other shapes constructed of stainless steel, other metals, ceramics, thermal plastics, or any other suitable material may be included in the volatilization chamber to aid in breaking up the plant material.
  • These milling objects are preferably sized such that they cannot exit the chamber and continue to rapidly spiral along the walls of the chamber, grinding and breaking up any large plant material particles.
  • an excluder screen or other exclusion device may be used to prevent any chance of the milling objects from exiting the chamber.
  • a non-limiting example of a few hollow milling balls 51 are illustrated in FIG. 8 a .
  • the exit of the volatilization chamber is designed and positioned such to serve as a particle classifier that allows only the smallest and lightest particles of plant material to leave the chamber.
  • the embodiment of the volatilization chamber illustrated in FIGS. 8 a and 8 b functions in a similar way to a cyclone separator in that it centrifugally excludes larger particles from leaving through the primary chamber exit 71 .
  • it is very different from a typical cyclone separator in that it does not have a secondary exit for captured particles to escape and that eventually all of the plant material particles do escape through the primary exit.
  • the plant material particles continue to circulate within the volatilization chamber until they are stripped of enough of their oils and are ground to a fine dust.
  • the plant material particles are carried out the main exit by the gas stream and eventually are separated by the primary plant material separator.
  • the embodiment of the volatilization chamber illustrated in FIGS. 8 a and 8 b may be used in parallel or in series with additional similar volatilization chambers or in combination with any of the other volatilization chambers described in this disclosure.
  • volatilization chamber While not illustrated in any figures in this disclosure, another embodiment of the volatilization chamber that may be preferred with some types of plant materials would consist of a pneumatic ring dryer design.
  • pneumatic ring dryer is well defined in industrial drying literature and the design of a ring dryer will be well known to those of skill in the art.
  • a ring dryer version of the volatilization chamber will have the benefit of allowing plant material to graduate through the system only after the desirable oils have been volatilized.
  • Other methods that may attain excellent volatilization of the plant oils may include spin flash drying systems, spin flash drying systems with agitator blades, rotating drum dryers, ball mill dryers, dryers with particle classifiers and other methods that will be known to those of skill in the art.
  • FIG. 9 illustrates a detailed view of an embodiment of the primary plant material separation device 8 and the secondary plant material entrainment section 27 .
  • the primary separation device is a cyclone separator. However, other centrifugal or non-centrifugal separation methods may be used.
  • the primary gas stream and entrained plant materials enter the primary plant material separation device through a tangential entrance 42 at the side of the separator 8 .
  • the entrained plant materials are centrifugally forced into contact with the outer walls 43 of the separator 8 , where they spiral down the walls 43 of the separator and fall from the bottom exit of the separator and eventually reach the processed plant material collection bin 29 .
  • one or more primary plant material separation devices may be used in parallel or in series or both in parallel and in series to obtain more complete separation of the entrained plant materials from the primary gas stream.
  • a cyclone separator is used as the primary plant material separation device, better separation can be achieved by the utilization of several small cyclones in parallel, each of a smaller diameter with a lower volume of gas flow, versus using one cyclone of a large diameter with a higher volume of gas flow. Placing cyclones in series also achieves better separation.
  • the separated plant material falls from the bottom exit of the separator 8 , it optionally passes through a specialized, heated and/or insulated exit tube 44 .
  • This heated exit tube 44 is also illustrated in the flow diagrams in FIG. 1 .
  • the processed plant material falls into the secondary entrainment section 27 where it is entrained in the secondary gas stream 25 and propelled into the secondary plant material separator 28 to eventually fall into the processed plant material collection bin 29 .
  • the secondary gas stream 25 be maintained at a lower temperature than the primary gas stream 1 , such that the processed plant material is cooled upon coming in contact with the secondary gas stream 25 .
  • a simple method of allowing the processed plant material to drop as a result of gravity or be mechanically propelled from the bottom of the primary plant material separator 8 into a bin or disposal area may be used to avoid the need for a secondary gas stream 25 and the parts required for a secondary gas stream system. If such an alternative is used, it may be preferable in some applications to provide an airlock valve, flapper valve or other method of isolating the primary plant material separator from the outside atmosphere.
  • This flow of atmospheric gas or displacing gas serves an important purpose—it prevents plant oil vapors from escaping from the exit of the primary plant material separator 8 and condensing on the parts within the secondary gas flow loop 25 and processed plant material bin 29 .
  • the heated exit tube 44 should be of sufficient length such that the vapor-free atmospheric or displacing gas is heated to near or greater than the volatilization temperature of the plant oils being volatilized prior to reaching the bottom portion of the primary plant material separator 8 .
  • the heat source for the heated exit tube 44 may be the heating jacket 36 described in the following paragraph, or a separate heating jacket that is heated by a similar method to the heating jacket 36 described in the following paragraph.
  • the heated exit tube 44 may be directly wrapped in an electric heating cable or similar device.
  • the displacing gas may also be heated by other methods.
  • One non-limiting example would be to place a spiraled atmospheric gas or displacing gas tube constructed of a metal, silicone or other heat resistant material in a heated area of the system or within the heated chamber that houses some or all of the heated components in some embodiments, such that the displacing gas is heated prior to being introduced to the separated plant material exit tube 44 .
  • Another non-limiting example would be to wrap a displacing gas or atmospheric displacing gas tube of suitable material in heating coils. Other methods may also be used to heat the gas being introduced to the separated plant material exit 44 . In cases where the method of displacing volatilized plant oils from the separated plant materials exit 44 are not effective or not deemed to be the best option, mechanical methods of removing accumulated plant oils from the plant material exit 44 and pathways to the separated plant material bin 29 may be employed. A few non-limiting examples include utilization of an auger screw or auger conveyor, rotating scraper blades, plunger pistons, a belt system or other methods that will be known to those of skill in the art.
  • both the processed plant material exit tube 44 and the primary plant material separator 8 are housed within a heating jacket 36 .
  • saturated steam of a specific pressure and temperature, a heated gas of a specific temperature or a heated thermal fluid of a specific temperature is pumped or otherwise introduced to the heating jacket through an entry passage 37 .
  • the steam and/or condensed steam, heated gas or thermal fluid circulates out of the heating jacket through an exit passage 38 .
  • the steam be supplied by the same steam generator that provides heat to the primary gas heater.
  • an electrical heat source within the jacket space or an electrical heating wire wrapped directly around the plant material separator 8 and/or exit tube may also be used.
  • the primary plant material separator in some embodiments of the primary plant material separator, it may be preferred to passively insulate the primary plant material separator 8 with a thermal insulation barrier such as fiberglass, ceramic wool, silica insulation, calcium silicate, aerogel, ceramic insulation, rock wool, mineral wool or any other suitable insulating medium. It may also be preferred in some applications to house the primary plant material separator 8 within a vacuum jacket. By way of example only, such a vacuum jacket would look substantially similar to the heating jacket 36 illustrated in FIG. 9 , except there would be no entry 37 or exit passages 38 for a heating medium. Instead, an evacuation passage would be included that may include a check valve or similar vacuum containment method.
  • the vacuum jacket may be permanently sealed or welded closed to retain the vacuum.
  • the primary plant material separator and/or separated plant material exit tube 44 may also be housed within an insulated and/or heated chamber with all or some of the heated components of the system. Such a method has been described in detail in other sections of this disclosure.
  • more efficient collection of the volatilized plant oils may occur through the utilization of a wetted packing material 81 .
  • a wetted packing material 81 Non-limiting examples of embodiments that utilize wetted packing materials are discussed in PCT/IB2014/002383, which is incorporated herein in its entirety, by reference.
  • FIG. 10 One example of a collection chamber containing wetted packing is illustrated in FIG. 10 .
  • Such an embodiment utilizing wetted packing may include a collection chamber 80 containing a wetted substrate 81 such as, but not limited to, random packing including raschig rings, saddles and beads made of glass, ceramics metals or other materials, other random packing materials such as sand, alumina, gravel, PTFE fibers, stainless steel wool, fiberglass or mineral wool fibers, and structured packing such as knitted packing, woven wire mesh, stainless steel wool, stainless steel matting, woven stainless steel mesh, corrugated metal sections, bubble-cap plates and sieve tray plates or other types of packing to capture the volatilized plant oils.
  • the packing material 81 may be wetted with collection solvent, which may collect the plant oils and eventually drip down through the packing material to the sump area 13 to be recovered.
  • the packing material may be wetted by collection solvent sprayers 82 or by other methods of contacting the packing material with collection solvent.
  • the wetted packing collection chamber 80 illustrated in FIG. 10 may also serve as the system's cooling chamber, with the sprayers 82 and/or packing material 81 serving to cool the gas stream.
  • a separate cooling chamber may be provided upstream of the collection chamber 80 , as is already illustrated in FIG. 10 .
  • a collection chamber with a wetted packing material may be used in other embodiments and in combination with collection chambers with collection solvent sprayers 17 or any other collection methods.
  • the location of the collection chamber 80 may also be varied depending on the application. As one non-limiting example, the wetted packing collection chamber 80 may be relocated to the position of the gas stream cooler 50 .
  • an electrostatic method of capturing condensed oil droplets may also be employed in the present invention.
  • an electrostatic scrubber the design of which will be readily known to those who are skilled in the art, may be placed after the cooling section 9 of the system. With this placement, the electrostatic collection plates may be optionally washed of collected oils by the falling collection solvent. The electrostatic collection plates may also be placed after the agglomeration section 14 or after the collection chamber section 16 and may be optionally washed with a spray of collection solvent. If efficient electrostatic collection occurs, it may be possible to reduce or eliminate some of the other collection methods throughout the system.
  • a centrifugal-type gas stream mover 19 capable of providing an outlet pressure of approximately 1.0 to 5.0 pounds per square inch is utilized to move the gas stream 1 throughout the system.
  • Other examples may include a gas stream mover capable of providing an outlet pressure of 0 to 150 pounds per square inch.
  • the gas stream mover 19 moves the gas stream 1 throughout the system at a flow rate of approximately 30 to 100 standard cubic feet per minute.
  • Other examples may include a gas stream mover capable of providing a flow rate of approximately 0.1 to 30 standard cubic feet per minute, 100 to 200 standard cubic feet per minute, 200 to 500 standard cubic feet per minute, over 500 cubic feet per minute or other ranges.
  • the gas stream As the gas stream passes through the gas stream heater 2 , the gas stream is heated to a temperature of approximately 290 to 430 degrees Fahrenheit. In other examples, the gas stream may be heated to a temperature range of approximately 100 to 300 degrees Fahrenheit, 100 to 310 degrees Fahrenheit, 200 to 300 degrees Fahrenheit, 200 to 310 degrees Fahrenheit, 280 to 450 degrees Fahrenheit, 300 to 500 degrees Fahrenheit, 300 to 400 degrees Fahrenheit, 300 to 370 degrees Fahrenheit, 300 to 365 degrees Fahrenheit, 305 to 360 degrees Fahrenheit, 300 to 360 degrees Fahrenheit, 300 to 330 degrees Fahrenheit, 310 to 320 degrees Fahrenheit, 340 to 370 degrees Fahrenheit, 350 to 360 degrees Fahrenheit, 350 to 365 degrees Fahrenheit, 415 to 445 degrees Fahrenheit, any combination of these temperature ranges or other temperature ranges.
  • Powdered or finely-ground plant material containing plant oils is fed into the gas stream 1 via an entrainment zone 6 at a rate of approximately 0.03 to 0.25 pounds per minute.
  • Other examples may include a feed rate of 0.001 to 0.03 pounds per minute, 0.25 to 1.0 pounds per minute, 1.0 to 5.0 pounds per minute, 5.0 to 10.0 pounds per minute, more than 10.0 pounds per minute or other feed rates.
  • the internal surface temperature of the extraction chamber 7 area and all areas of the system that contact the gas stream as the gas stream passes between the gas stream heater 2 and the gas stream cooling section 9 are kept above the condensation temperature of the volatilized oils or near the temperature of the gas stream exiting the heater 2 to prevent condensation of plant oils on these surfaces.
  • this temperature is kept near or above approximately 290 to 430 degrees Fahrenheit. In other examples, the temperature may be kept in a range of approximately 100 to 300 degrees Fahrenheit, 100 to 310 degrees Fahrenheit, 200 to 300 degrees Fahrenheit, 200 to 310 degrees Fahrenheit, 280 to 450 degrees Fahrenheit, 300 to 500 degrees Fahrenheit, 300 to 400 degrees Fahrenheit, 300 to 370 degrees Fahrenheit, 300 to 365 degrees Fahrenheit, 305 to 360 degrees Fahrenheit, 300 to 360 degrees Fahrenheit, 300 to 330 degrees Fahrenheit, 310 to 320 degrees Fahrenheit, 340 to 370 degrees Fahrenheit, 350 to 360 degrees Fahrenheit, 350 to 365 degrees Fahrenheit, 415 to 445 degrees Fahrenheit, any combination of these temperature ranges or other temperature ranges.
  • the evaporation device 31 is operable to distill approximately 0.04 to 0.15 gallons per minute of collection solvent from the mixture of plant oils and collection solvent. Other examples may include separation rates of approximately 0.0002 to 0.04 gallons per minute, 0.15 to 0.5 gallons per minute, 0.5 to 1.0 gallons per minute, 1.0 to 5.0 gallons per minute, 5.0 to 10.0 gallons per minute, more than 10.0 gallons per minute or other rates.
  • the distilled collection solvent is stored in a separate reservoir 56 from the sump reservoir area 13 .
  • a substantially purified flow of collection solvent is pumped to the cooling spray 10 at a rate of approximately 0.03 to 1.0 gallons per minute.
  • Other examples may include rates of 0.0002 to 0.03 gallons per minute, 1.0 to 7.0 gallons per minute, 7.0 to 10.0 gallons per minute, greater than 10.0 gallons per minute, less than 10.0 gallons per minute or other rates.
  • the cooling spray cools the gas stream to approximately 160 to 180 degrees Fahrenheit.
  • the cooling spray cools the gas stream to approximately 80 to 150 degrees Fahrenheit, 0 to 150 degrees Fahrenheit, 0 to 100 degrees Fahrenheit, 40 to 80 degrees Fahrenheit, less than 180 degrees Fahrenheit, less than 173 degrees Fahrenheit, less than 150 degrees Fahrenheit, less than 140 degrees Fahrenheit, less than 130 degrees Fahrenheit, less than 120 degrees Fahrenheit, less than 110 degrees Fahrenheit, less than 100 degrees Fahrenheit or other temperatures.
  • the gas stream and entrained liquids pass through the primary gas stream cooler 50 .
  • the gas stream cooler 50 cools the gas stream and entrained liquids/oils to approximately 90 to 150 degrees Fahrenheit.
  • the gas stream cooler cools the gas stream and entrained liquids/oils to approximately 0 to 150 degrees Fahrenheit, 0 to 100 degrees Fahrenheit, 40 to 80 degrees, 0 to 90 degrees Fahrenheit, less than 150 degrees Fahrenheit, less than 140 degrees Fahrenheit, less than 130 degrees Fahrenheit, less than 120 degrees Fahrenheit, less than 110 degrees Fahrenheit, less than 100 degrees Fahrenheit, less than 90 degrees Fahrenheit, less than 80 degrees Fahrenheit, or other temperatures.
  • these sections may be operable to cool the gas stream and entrained liquids/oils to approximately 90 to 150 degrees Fahrenheit or any of the temperature ranges listed above for the cooling spray or gas stream cooler.
  • the collection solvent may be cooled to a temperature less than the boiling point of the collection solvent being used.
  • the collection solvent cooler such as 55 , may cool the collection solvent to a temperature of approximately 0 to 150 degrees Fahrenheit, 0 to 40 degrees Fahrenheit, 40 to 80 degrees Fahrenheit, 80 to 120 degrees Fahrenheit, to less than 100 Fahrenheit, to less than 120 degrees Fahrenheit, to less than 150 degrees Fahrenheit or other temperature ranges.
  • all of the internal areas of the system that contact the gas stream as the gas stream passes between the gas stream cooler 50 and the gas stream heater 2 are kept at a temperature that is below the temperature of the gas stream when it exits the gas stream cooler 50 , such that collection solvent condenses on these surfaces to wash away any accumulated plant oils.
  • the temperature is kept near or below 85 to 145 degrees Fahrenheit.
  • the primary solvent pump 12 pumps collection solvent from the sump area 13 to the collection solvent sprayers 17 in the collection chamber 16 at a rate of approximately 1.0 to 7.0 gallons per minute.
  • the collection solvent used within the system may be comprised primarily of ethyl alcohol and water at a ratio of approximately 40% ethyl alcohol and 60% water to 95% ethyl alcohol and 5% water.
  • the evacuation pump 24 is operable to maintain a negative system pressure such that the highest pressure area of the gas stream (such as that found at the blower exit) is still kept slightly below that of ambient pressure.
  • the volume of gas displaced by the evacuation pump 24 is approximately 0.01 to 5.0 cubic feet per minute.
  • FIG. 2 shows several of the parts of the system rearranged or even eliminated.
  • FIG. 2 shows that the centrifugal droplet separator 20 illustrated in FIG. 1 has been removed.
  • the steam generator 3 has also been removed in FIG. 2 .
  • electric heating elements are used in the heater section 2 .
  • the plant material collection system has also been simplified. Instead of utilizing a secondary entrainment zone 27 and a secondary gas stream 25 , the primary plant material separation device drains directly into the processed plant material collection bin 29 .
  • An optional airlock valve 58 may be used to keep the processed plant material collection bin 29 separated from the primary gas stream 1 .
  • Two gas movers 19 have been used in series to increase the pressure available to propel the gas stream.
  • the placement of one of the gas movers 19 has been moved from the position illustrated in FIG. 1 , however, this could be placed directly in front of the second gas mover 19 or elsewhere in the system.
  • FIG. 11 illustrates an embodiment of the invention that is designed to operate without a collection solvent.
  • This embodiment may be operated with no solvent at all, or with only a minimal amount of a diluting solvent.
  • This embodiment includes a primary gas stream 1 , a tube-in-shell steam powered gas stream heater 2 , a steam generator 3 to provide steam to the heater, a gas stream mover 19 , a hopper 4 , a plant material portioning device 5 , a primary plant material entrainment zone 6 , one or more volatilization chambers 7 , a primary plant material separation device 8 , a gas stream filter 49 , a volatilized oil condenser/gas stream cooler 50 , a condensed plant oil gas stream/oil separation device 82 , an oil collection area 32 , a heated separated plant material exit 44 , an air pump 24 capable of removing a portioned amount of gas from the system, a secondary gas stream 25 , a secondary gas stream mover 26 , a secondary plant material
  • any of these components and parts may be duplicated within the system one or more times in series or in parallel or may be eliminated entirely to attain different effects.
  • the order of the components within the system may also be modified to attain different effects.
  • the steam powered heater 2 may also be replaced with an electrically powered heater, a heater with a circulating thermal fluid, or a heater that is powered by other methods.
  • Elements 1 , 2 , 3 , 19 , 4 , 5 , 6 , 7 , 8 , 49 , 44 , 25 , 26 , 27 , 28 , 29 , 30 , 22 , 23 , and 24 function in a substantially similar manner to corresponding similar components in previously discussed embodiments of the invention.
  • Element 50 functions in a modified way as compared to previously discussed embodiments. Additionally, in some embodiments, the gas stream mover has been placed after the heater such that it remains too hot for plant oils to condense on its inner surfaces. It should be noted that the elements mentioned may also function in a similar way in the embodiments following this section.
  • the embodiment illustrated in FIG. 11 is designed to use little or no solvent.
  • the volatilized plant oils travel from the volatilization section 7 , through the primary plant material separation device 8 and through the optional gas stream filter 49 , they enter a volatilized oil condenser/gas stream cooling section 50 .
  • the condenser/gas stream cooler 50 is preferably a tube-in-shell heat exchanger that is cooled by a coolant or coolant mixture, however, any of the condenser designs and cooling methods previously discussed within this document or PCT/IB2014/002383 may be used.
  • the volatilized oils enter the gas stream condenser/cooler 50 , a portion of the volatilized oils condense on the condensation surfaces within the condenser.
  • the volatilized oils that do not condense through the first pass through the condenser may continue to recirculate with the gas stream until they are condensed in successive passes through the condenser 50 .
  • the extracted plant oils that condense on the condensation surfaces within the condenser 50 drip down the condenser surfaces and flow out of the condenser 50 into a condensed oil separation section 82 and eventually into the condensed oil collection area 32 .
  • the gas stream 1 continues to flow through the system and back through the heater.
  • a few non-limiting temperature examples may include maintaining the condensation surfaces within the condenser between 100 to 300 degrees Fahrenheit, 120 to 280 degrees Fahrenheit, 120 to 150 degrees Fahrenheit, and 320 to 340 degrees Fahrenheit. Other temperatures ranges may also be used.
  • FIG. 12 a illustrates another embodiment of the invention that needs little or no solvent to function.
  • a centrifugal condensed oil separator 83 is utilized.
  • the centrifugal oil separator 83 may be a cyclone or other suitable separation device.
  • As the gas stream passes through the gas stream condenser/cooler 50 a portion of the volatilized plant oils will condense on the surfaces within the condenser, however, a portion of the oil may also condense and precipitate into the cooler gas stream as small or microscopic oil droplets that become entrained in the flow of the gas stream.
  • FIG. 12 a In order to illustrate that many of the components within the invention may be rearranged or altered in different applications, the embodiment illustrated in FIG. 12 a is shown with a simplified processed plant material collection system as compared to FIG. 11 .
  • FIG. 12 b illustrates an arrangement similar to the embodiment illustrated in FIG. 12 a .
  • the gas stream mover 19 is placed after the condenser/cooler 50 and before the heater 2 .
  • An optional condensed oil separation section 82 may be included in this embodiment.
  • the gas stream mover be of a centrifugal blower design, such as, but not limited to a regenerative blower, turbine blower, pressure blower, turbo compressor, centrifugal blower or any other design capable of creating suitable centrifugal forces.
  • the gas stream mover 19 serves as a centrifugal oil separator that separates and collects microscopic oil droplets that precipitated into the gas stream after the gas stream was cooled.
  • a gas stream mover with blades e.g., a turbo compressor, regenerative blower, turbine blower, pressure blower or a gas stream mover with high speed parts
  • Such a blower may be substituted for any of the gas stream mover elements discussed in this document.
  • the centrifugal oil separator 83 or centrifugal gas stream mover 19 be maintained at a temperature that is high enough to keep the captured droplets runny and free flowing so the collected oil may flow from the centrifugal capture device, yet cool enough to prevent any of the captured oil droplets from being re-volatilized. It is also preferable that the condenser/gas stream cooler 50 in the embodiments illustrated in FIGS.
  • FIGS. 12 a and 12 b it may be preferred to design the gas stream cooler 50 to minimize the quantity of oil collected in the condenser and rely primarily on the centrifugal separator 83 or centrifugal gas mover 19 as the primary separation device.
  • FIG. 13 illustrates another embodiment that is designed to use little or no solvent to function.
  • a set of elements that includes a gas stream condenser/cooler 50 , an oil separator 82 and an extracted oil collection area 32 is repeated in series as many times as is practical to remove various fractions from the volatilized oils within the gas stream. With this arrangement, fractionalization of the plant oil constituents may occur in a continuous manner.
  • FIG. 13 only two sets of gas stream condensers/coolers 50 , oil separation sections 82 and extracted oil collection areas 32 are illustrated in FIG. 13 , however, this number may be increased. In the embodiment illustrated in FIG.
  • the heater 2 it will be beneficial to set the heater 2 to a temperature that is high enough to volatilize all of the desired fractions within the plant material to be extracted, such that all of the oil fractions become volatilized and travel within the gas stream 1 as volatilized plant oil gasses.
  • the condensation surfaces within the first gas stream condenser/cooler 50 should be maintained at a temperature that is low enough to condense a first fraction of volatilized plant oil constituents and yet is too high to condense other fractions of volatilized plant oil constituents.
  • the first fraction of volatilized plant oils will condense on the condenser surfaces and drain through the first condenser 50 , through the first oil separator 82 and into first oil collection area 32 .
  • This pattern may be repeated with multiple gas stream condenser/coolers as many times as is practical to remove various fractions from the volatilized oils within the gas stream. It is beneficial that the last condenser 50 in the series be maintained at a low enough temperature to condense all of the remaining oil fractions and yet still be kept hot enough to keep the oils flowing freely from the last condenser, through the last oil separator 82 and into the last extracted oil collection area 32 .
  • FIG. 14 illustrates an additional embodiment that enables continuous fractionalization.
  • the last oil separation device in the series is a centrifugal oil separation device 83 , as previously described in the section describing FIG. 12 a .
  • a centrifugal separation device 83 may be placed after each successive condenser/gas stream cooler 50 to facilitate collection of the fractionated oil components in a similar way as described in FIG. 12 a.
  • FIG. 15 illustrates an additional embodiment that enables continuous fractionalization.
  • the gas stream mover 19 has been relocated to serve as a centrifugal oil separation device.
  • centrifugal gas movers have been previously discussed in other sections of this disclosure.
  • a few non-limiting examples may include turbo compressors, regenerative blowers, turbo blowers, pressure blowers and other centrifugal devices.
  • a centrifugal gas stream mover 19 may be placed after each successive condenser 50 to facilitate collection of the fractionated oil components.
  • the internal areas of the volatilization chamber may be heated to a temperature between 356 and 440 degrees Fahrenheit to volatilize all of the desired fractions of plant oil to be extracted.
  • the condensation surfaces within a first gas stream condenser/cooler 50 may be maintained between 366 and 427 degrees Fahrenheit.
  • the condensation surfaces within a second gas stream condenser/cooler may be maintained between 357 and 364 degrees Fahrenheit.
  • the condensation surfaces within a third gas stream condenser/cooler 50 may be maintained between 316 and 355 degrees Fahrenheit.
  • the condensation surfaces within a fourth gas stream condenser/cooler 50 may be maintained between 290 and 314 degrees Fahrenheit.
  • the condensation surfaces within a final gas stream condenser/cooler 50 may be maintained between 110 and 289 degrees Fahrenheit.
  • Other temperatures and numbers of repeating components may be used in other embodiments and examples.
  • the internal areas of the volatilization chamber may be heated to a temperature between 356 and 400 degrees Fahrenheit to volatilize all of the desired fractions of plant oil to be extracted.
  • the condensation surfaces within a first gas stream condenser/cooler 50 may be maintained between 357 and 364 degrees Fahrenheit.
  • the condensation surfaces within a second gas stream condenser/cooler may be maintained between 316 and 355 degrees Fahrenheit.
  • the condensation surfaces within a third gas stream condenser/cooler 50 may be maintained between 290 and 314 degrees Fahrenheit.
  • the condensation surfaces within a final gas stream condenser/cooler 50 may be maintained between 110 and 289 degrees Fahrenheit.
  • Other temperatures and numbers of repeating components may be used in other embodiments and examples.
  • FIG. 16 illustrates an embodiment that utilizes an electrostatic collector 84 to efficiently remove plant oil from the gas stream.
  • an electrostatic collector 84 to efficiently remove plant oil from the gas stream.
  • a portion of the volatilized plant oils may condense on the surfaces within the condenser and drip down through the system and into the extracted oil collection area 32 , while another portion of the oil may condense and precipitate into the cooler gas stream as small or microscopic oil droplets that become entrained in the flow of the gas stream.
  • an electrostatic collector 84 a large portion of these entrained small and microscopic oil droplets may be captured within the electrostatic collector prior to being recirculated back through the heater 2 .
  • the electrostatic collector 84 imparts an electrostatic charge to the entrained oil droplets.
  • the collection surfaces within the electrostatic collector 84 are charged with an opposite electrostatic charge from the oil droplets.
  • the oil droplets are electrically attracted to the collection surfaces.
  • the oil droplets collect on the collection surfaces, they begin to coalesce into larger droplets that drip from the electrostatic collection surfaces and drain through the system into the extracted oil collection area 32 .
  • the design and function of electrostatic collectors will be known to those of skill in the art.
  • condensation surfaces within the gas stream condenser/cooler 50 be maintained at a temperature below the condensation point of the volatilized plant oils being extracted and yet high enough to keep the plant oils in a runny state so they readily drip and flow out of the bottom of the condenser 50 , through the electrostatic collector 84 , through the condensed oil separation section 82 and into the condensed oil collection area 32 .
  • the gas stream exiting the gas stream condenser/cooler 50 be maintained at a temperature that keeps the surfaces of the electrostatic collector 84 warm enough that collected oil may freely drip from the electrostatic collection surfaces and drain down through the system to the oil collection area 32 .
  • a few non-limiting temperature examples may include maintaining the condensation surfaces within the condenser 50 and electrostatic collector area 84 between 100 to 300 degrees Fahrenheit, 120 to 280 degrees Fahrenheit, 120 to 150 degrees Fahrenheit, and 320 to 340 degrees Fahrenheit.
  • FIG. 17 illustrates an embodiment that utilizes a filtration section 85 that includes filters, demisting pads and/or packing material to remove small and microscopic oil droplets from the gas stream.
  • the mediums contained in the filtration section 85 are designed to function with little or no solvent. Since there may be little or no solvent present, it is preferred that the filtration section be maintained at a temperature that keeps the collected oil runny and free flowing so as to allow the oil to easily drip from the filter and/or demisting pads and into the extracted oil collection area 32 .
  • a portion of the volatilized plant oil may condense on surfaces within the condenser and drip down through the system and into the extracted oil collection area 32 , while another portion of the oil may condense and precipitate into the cooler gas stream as small or microscopic oil droplets that become entrained in the flow of the gas stream.
  • the gas stream and entrained small and microscopic plant oil droplets pass from the gas stream condenser 50 and pass through the filtration section 85 , a portion of the entrained oil droplets may be removed from the gas stream.
  • the filtration material may comprise a number of materials, such as, but not limited to sintered glass filters, sintered ceramic filters, sintered metal filters, ceramic filters, other filter designs, random and/or inert packing including raschig rings, saddles and beads made of glass, ceramics, metals, other random and/or inert packing materials such as sand, alumina, gravel, PTFE fibers, stainless steel wool, glass fibers or mineral wool fibers, and structured packing such as knitted packing, woven wire mesh, stainless steel wool, stainless steel matting, woven stainless steel mesh, corrugated metal sections, bubble-cap plates and sieve tray plates or other types of packing to capture the volatilized plant oils.
  • the demisting material may comprise any of the preceding materials, or the demisting material may comprise a structured demister design, corrugated plates demister design, or other design.
  • Portions of the systems in FIGS. 11, 12 a , 12 b , 13 , 14 , 15 , 16 and 17 may be heated and/or insulated to assist in achieving target temperatures and/or to prevent condensation in certain areas of the system.
  • any of the embodiments illustrated in FIGS. 11, 12 a , 12 b , 13 , 14 , 15 , 16 and 17 and discussed in their accompanying text may use little or no solvent to function. In some cases, it may be preferred to use no-solvent. In some cases, it may be preferred to use a minimal amount of solvent, not as a primary collection method, but as a diluent or thinning agent to maintain a liquefied oil in a free-flowing state such that it freely drains from the invention's various collection and separation devices. In cases where a minimal amount of solvent is utilized, the general goal is to use as little as possible.
  • a few non-limiting examples would be to use a sufficient amount of solvent such that the collected oils can be measured to contain 25% or less solvent by weight, 15% or less solvent by weight or 10% or less solvent by weight. It may also be advantageous in some cases to maintain a certain level of dissolved solvent in the gas stream. A few non-limiting examples would be to use a sufficient amount of solvent such that the gas stream can be measured to contain 25% or less solvent vapor by weight, 15% or less solvent vapor by weight or 10% or less solvent vapor by weight. In other cases, it may be preferred to maintain a much higher ratio of diluting solvent to ensure that the collected oils do not become too thick to be removed from the system.
  • the introduction of diluting solvent to the embodiments illustrated in FIGS. 11, 12 a , 12 b , 13 , 14 , 15 , 16 and 17 may be before and/or within the gas stream cooler 50 , before and/or within the centrifugal collection device section 83 , before and/or within the centrifugal gas stream mover collection section 19 , before and/or within the electrostatic collection section 84 , before and/or within the filter collection section 85 , before and/or within the oil separation section 82 , and/or within other sections of the system.
  • the diluting solvent may be advantageous to introduce as a vapor instead of a liquid, with the point of introduction being placed in any of the sections previously stated, within the gas stream 1 , within the gas stream heater 2 , within the extraction chamber 7 , within the gas stream mover 19 , within the gas stream filter 49 , within the plant material separation device 8 , and/or anywhere within the system.
  • the method of introduction of a diluting solvent may be via a nozzle, tube, sprayer, valve, gas injector or any other method known to those of skill in the art or described in other parts of this disclosure.
  • the diluting solvent utilized in the embodiments illustrated in FIGS. 11, 12 a , 12 b , 13 , 14 , 15 , 16 and 17 may consist of ethanol, a mixture of ethanol and water, or may consist of any of compounds that are used as collection solvents in any other embodiments described within this disclosure or PCT/IB2014/002383, or other solvents, or a mixture of various solvents. It is preferred that the diluting solvent be food or medical grade, however any suitable diluting solvent may be used.
  • ethanol diluting solvent that is about 100% ethanol, about 95% ethanol and 5% water, about 90% ethanol and 10% water, about 85% ethanol and 15% water, about 80% ethanol and 20%, water, about 75% ethanol and 25% water, about 70% ethanol and 30% water, about 65% ethanol and 35% water, about 60% ethanol and 40% water, about 55% ethanol and 45% water, about 50% ethanol and 50% water, or ethanol and water at other ratios.
  • a mixture of ethanol and water may be introduced with an ethanol concentration that is greater than 40% ethanol, greater than 50% ethanol, greater than 55% ethanol, greater than 65% ethanol, greater than 70% ethanol, greater than 75% ethanol, greater than 80% ethanol, greater than 85% ethanol, greater than 90% ethanol or greater than 95% ethanol.
  • Ethanol may also be mixed with other solvents at various ratios. The specific descriptions in this disclosure should not be viewed as limiting the scope of this invention. The elements within the embodiments illustrated in FIGS.
  • the volatilization chamber 7 is shown with a bottom entrance and a top exit but may have the entrance and exit located elsewhere. It should be noted that the gas stream condenser/cooler 50 and electrostatic collector 84 may be combined into the same section in some embodiments. It should also be noted that the gas stream heater 2 may be powered by electric heating elements instead of steam or a heated fluid. Other condenser designs may be used. Any of the components described in FIGS. 11, 12 a , 12 b , 13 , 14 , 15 , 16 and 17 and their accompanying text may be modified in any way that similar components are described in other embodiments within this disclosure, PCT/IB2014/002383, or in other ways that are generally known to those of skill in the art.
  • FIGS. 11, 12 a , 12 b , 13 , 14 , 15 , 16 and 17 it may be advantageous to operate the embodiments in FIGS. 11, 12 a , 12 b , 13 , 14 , 15 , 16 and 17 as open systems.
  • the system it is preferable that the system be open after the final oil droplet separator/collection device ( 83 , 19 , 84 , 85 or 82 ) and before the heater 2 .
  • the disclosure relates to a method of extracting oil from plant material.
  • the method may comprise providing a system for extracting oil from plant material.
  • the system may comprise a gas moving device operable to propel a gas stream through the system.
  • the system may comprise an extraction chamber in communication with the gas moving device such that the gas stream is directed through the extraction chamber.
  • the system may comprise a condensation surface in communication with the gas moving device such that the gas stream is directed to the condensation surface.
  • the gas moving device may or may not be a centrifugal separator.
  • the gas mover may or may not comprise a compressed air tank or a liquefied gas, such as liquid nitrogen.
  • the condensation surface may be a surface configured to allow the portion of oil to flow along the surface to allow collection of the oil.
  • the condensation surface may therefore comprise chemical and/or mechanical properties that allow the portion of oil to flow.
  • a condensation surface that allows the portion of oil to flow provides an advantage over existing systems because it allows methods that use less solvent.
  • the system may comprise a centrifugal separator, which may comprise the condensation surface.
  • the centrifugal separator may or may not be the gas moving device of the system.
  • the centrifugal separator may comprise at least one blade and an axis of rotation, e.g., such that the at least one blade rotates about the axis, or the centrifugal separator may comprise a device with no blades at all.
  • the method may further comprise rotating the blade about the axis.
  • the condensation surface may comprise the at least one blade and/or may comprise a surface of the centrifugal separator other than a blade such as the housing of the separator.
  • the method may further comprise maintaining the at least one blade at both a temperature and an angular velocity that results in a centrifugal force that is greater than the resistance of the portion of the oil to flow.
  • the rotation of the blade about the axis may thereby provide a mechanical force that causes the portion of the oil to flow such that the oil may be collected.
  • the condensation surface does not comprise a blade of the centrifugal separator.
  • a system may comprise a centrifugal separator that lacks blades, or a system may comprise a centrifugal separator having one or more blades wherein the condensation surface does not comprise the one or more blades.
  • the system may comprise a condensation surface that is heated and/or angled to allow the portion of oil to flow.
  • a method may comprise maintaining a condensation surface at an angle and temperature that result in a parallel component of gravitational force that is greater than the resistance of the portion of the oil to flow.
  • the condensation surface may be angled of about ⁇ 90° to about 90° relative to the force of gravity, such as about ⁇ 90° to about ⁇ 70°, about ⁇ 80° to about ⁇ 600, about ⁇ 70° to about ⁇ 50°, about ⁇ 60° to about ⁇ 40°, about ⁇ 50° to about ⁇ 30°, about ⁇ 40° to about ⁇ 20°, about ⁇ 30° to about ⁇ 10°, about ⁇ 20° to about 0°, about ⁇ 10° to about 10°, about 0° to about 20°, about 10° to about 30°, about 20° to about 40°, about 30° to about 50°, about 40° to about 60°, about 50° to about 70°, about 60° to about 80°, or about 70° to about 90°.
  • Surfaces of less than 0° to about ⁇ 90° are ceilings, a surface of 0° is a wall that is parallel to the force of gravity, and surfaces of greater than 0° to less than 90° are inclined planes.
  • the condensation surface may be angled at about ⁇ 90° to about 60°, about 0° to about 60°, about 0° to about 45°, or about ⁇ 45° to about 45° relative to the force of gravity.
  • a condensation surface may comprise an electrostatic charge.
  • the electrostatic charge may be sufficient to capture and remove a portion of the oil from the gas stream.
  • the method may further comprise condensing the portion of the oil into oil droplets that become entrained in the gas stream after volatizing the oil.
  • the method comprises charging the oil droplets with an electrostatic charge (e.g., a charge that is opposite from the charge of the condensation surface).
  • Contacting the gas stream with the condensation surface may comprise contacting the charged oil droplets with the condensation surface.
  • a condensation surface may comprise a filter medium and/or demisting pad.
  • the filter medium and/or demisting pad may be sufficient to capture and remove a portion of the oil from the gas stream.
  • the method may further comprise condensing the portion of the oil into oil droplets that become entrained in the gas stream after volatizing the oil.
  • the temperature of a condensation surface, centrifugal separator, centrifugal capture device, centrifugal gas stream mover, electrostatic collector, filter section, condenser, and/or gas stream cooler is about 100° F. to about 300° F., about 110° F. to about 289° F., about 120° F. to about 280° F., about 120° F. to about 150° F., about 290° F. to about 314° F., about 316° F. to about 355° F., about 320° F. to about 340° F., about 357° F. to about 364° F., or about 366° F. to about 427° F.
  • the temperature of a condensation surface, centrifugal separator, centrifugal capture device, centrifugal gas stream mover, electrostatic collector, filter section, condenser, and/or gas stream cooler may be about 100° F. to about 315° F., about 100° F. to about 212° F., or about 120° F. to about 315° F.
  • the temperature of a condensation surface, centrifugal separator, centrifugal capture device, centrifugal gas stream mover, electrostatic collector, filter section, condenser, and/or gas stream cooler may be about 100° F. to about 140° F., about 120° F. to about 160° F., about 140° F. to about 180° F., about 160° F.
  • a system may comprise more than one condensation or collection surface, and one condensation or collection surface may be kept at a different temperature than another condensation or collection surface.
  • any of the temperature ranges infra may be used interchangeably with different components.
  • centrifugal collection device section 83 centrifugal gas stream mover collection section 19 , electrostatic collection section 84 or filter collection section 85 may be kept at a warmer temperature during operation through active heating (for example, at one of the warmer temperature ranges described), or may be allowed to assume the temperature of the gas stream after it has passed through the cooler and then be intermittently heated during or after operation to facilitate removal of the collected oils. Additionally, if the gas stream cooler is found to collect oils that are too cold to flow, it also may be intermittently heated during or after operation to allow the collected oils to flow from the gas stream cooler/condenser section 50 .
  • the method may comprise maintaining the temperature of the condensation surface at about 100° F. to about 300° F., about 110° F. to about 289° F., about 120° F. to about 280° F., about 120° F. to about 150° F., about 290° F. to about 314° F., about 316° F. to about 355° F., about 320° F. to about 340° F., about 357° F. to about 364° F., or about 366° F. to about 427° F.
  • the method comprises maintaining the temperature of the condensation surface at about 100° F. to about 315° F., about 100° F. to about 212° F., or about 120° F. to about 315° F.
  • the method may comprise maintaining the temperature of the condensation surface at about 100° F. to about 140° F., about 120° F. to about 160° F., about 140° F. to about 180° F., about 160° F. to about 200° F., about 180° F. to about 220° F., about 200° F. to about 240° F., about 220° F. to about 260° F., about 240° F. to about 280° F., about 260° F. to about 300° F., about 280° F. to about 320° F., about 300° F. to about 340° F., about 320° F. to about 360° F., about 340° F. to about 380° F., about 360° F. to about 400° F., about 380° F. to about 420° F., or about 400° F. to about 440° F.
  • the preferred method may be to keep some condensation or collection surfaces at different temperatures than other condensation or collection surfaces.
  • any of the temperature ranges infra may be used interchangeably with different components.
  • cooling the gas stream containing the oil comprises cooling the gas stream to a temperature that is at least about 5° F., 10° F., 15° F., 20° F., 25° F., 30° F., 35° F., 40° F., 45° F., or 50° F. lower than the temperature of the condensation surface.
  • the relatively lower temperature of the gas stream may help condense the gas whereas the relatively higher temperature of the condensation surface may help ensure that the oil remains fluid enough to be collected.
  • cooling the gas stream containing the oil comprises cooling the gas stream to a temperature that is at least about 5° F., 10° F., 15° F., 20° F., 25° F., 30° F., 35° F., 40° F., 45° F., or 50° F. higher than the temperature of the condensation surface.
  • the relatively higher temperature of the gas stream may help ensure that the oil does not condense prior to contacting the condensation surface.
  • a method may comprise changing the temperature of the condensation surface.
  • a method may comprise increasing the temperature of the condensation surface.
  • the temperature may be increased to decrease the resistance of the portion of the oil to flow, e.g., to increase the rate at which the oil is collected from the condensation surface.
  • the temperature may be increased, for example, in response to oil build-up on the condensation surface.
  • a method may comprise decreasing the temperature of the condensation surface. The temperature may be decreased, for example to increase the rate at which the condensation surface captures and removes the portion of oil from the gas stream.
  • the method may comprise providing a plant material in the extraction chamber, propelling the gas stream through the extraction chamber, and volatizing an oil from the plant material such that the oil is extracted from the plant material and into the gas stream.
  • the method may comprise cooling the gas stream containing the oil and propelling the gas stream containing the oil to the condensation surface.
  • the method may comprise contacting the gas stream with the condensation surface thereby capturing and removing a portion of the oil from the gas stream.
  • the method may comprise collecting the portion of the oil from the condensation surface thereby producing a collected oil.
  • the gas stream may comprise less than about 30%, about 25%, about 20%, about 15%, about 10%, about 9%, about 8%, about 7%, about 6%, about 5%, about 4%, about 3%, about 2%, or about 1% solvent vapor by weight.
  • the gas stream may comprise less than about 30%, about 25%, about 20%, about 15%, about 10%, about 9%, about 8%, about 7%, about 6%, about 5%, about 4%, about 3%, about 2%, or about 1% solvent vapor by weight prior to propelling the gas stream through the extraction chamber, after propelling the gas stream through the extraction chamber, prior to volatizing the oil, after volatizing the oil, prior to cooling the gas stream, after cooling the gas stream, prior to contacting the gas stream with the condensation surface, after contacting the gas stream with the condensation surface, prior to collecting the portion of oil, and/or after collecting the portion of oil.
  • the portion of the oil captured and removed from the gas stream may comprise less than about 30%, about 25%, about 20%, about 15%, about 10%, about 9%, about 8%, about 7%, about 6%, about 5%, about 4%, about 3%, about 2%, or about 1% solvent by weight.
  • the portion of the oil captured and removed from the gas stream may comprise less than about 30%, about 25%, about 20%, about 15%, about 10%, about 9%, about 8%, about 7%, about 6%, about 5%, about 4%, about 3%, about 2%, or about 1% solvent by weight after contacting the gas stream with the condensation surface, prior to collecting the portion of oil, and/or after collecting the portion of oil.
  • the collected oil may comprise less than about 30%, about 25%, about 20%, about 15%, about 10%, about 9%, about 8%, about 7%, about 6%, about 5%, about 4%, about 3%, about 2%, or about 1% solvent by weight.
  • the ratio of solvent to oil may be increased to any higher ratio as needed.
  • the portion of the oil captured and removed from the gas stream may comprise a dilution solvent to oil ratio of about 25:1 to 20:1, about 20:1 to 15:1, about 15:1 to about 10:1, about 10:1, about 9:1, about 8:1, about 7:1, about 6:1, about 5:1, about 4:1 about 3:1 about 2:1 or about 1:1.
  • the portion of the oil captured and removed from the gas stream may comprise a solvent to oil ratio of about 25:1 to 20:1, about 20:1 to 15:1, about 15:1 to about 10:1, about 10:1, about 9:1, about 8:1, about 7:1, about 6:1, about 5:1, about 4:1 about 3:1 about 2:1 or about 1:1 after contacting the gas stream with the condensation surface, prior to collecting the portion of oil, and/or after collecting the portion of oil.
  • the collected oil may comprise a solvent to oil ratio of about 25:1 to 20:1, about 20:1 to 15:1, about 15:1 to about 10:1, about 10:1, about 9:1, about 8:1, about 7:1, about 6:1, about 5:1, about 4:1 about 3:1 about 2:1 or about 1:1.
  • the gas stream may comprise a dilution solvent to oil ratio of about 25:1 to 20:1, about 20:1 to 15:1, about 15:1 to about 10:1, about 10:1, about 9:1, about 8:1, about 7:1, about 6:1, about 5:1, about 4:1 about 3:1 about 2:1 or about 1:1.
  • the gas stream may comprise a solvent to oil ratio of about 25:1 to 20:1, about 20:1 to 15:1, about 15:1 to about 10:1, about 10:1, about 9:1, about 8:1, about 7:1, about 6:1, about 5:1, about 4:1 about 3:1 about 2:1 or about 1:1 prior to propelling the gas stream through the extraction chamber, after propelling the gas stream through the extraction chamber, prior to volatizing the oil, after volatizing the oil, prior to cooling the gas stream, after cooling the gas stream, prior to contacting the gas stream with the condensation surface, after contacting the gas stream with the condensation surface, prior to collecting the portion of oil, and/or after collecting the portion of oil.
  • the gas stream, portion of the oil, and/or collected oil may comprise little solvent, and/or the gas stream, portion of the oil, or collected oil may be essentially free of solvent. “Essentially free” means that the gas stream, portion of the oil, and/or collected oil may contain unavoidable impurities from the starting materials (e.g., plant material and gas stream) but that the gas stream, portion of the oil, or collected oil are otherwise free from solvent. In some embodiments, the gas stream, portion of the oil, and/or collected oil comprise no solvent. The gas stream, portion of the oil, and/or collected oil may be essentially free of isobutane, ethanol, and/or chloroform.
  • contacting the gas stream with the condensation surface comprises contacting a vapor of the oil with the condensation surface. Contacting the gas stream with the condensation surface may cause the portion of the oil to condense on the condensation surface.
  • the method further comprises condensing the portion of the oil into oil droplets that become entrained in the gas stream after cooling the gas stream.
  • Contacting the gas stream with the condensation surface may comprise contacting the oil droplets with the condensation surface, which may cause the oil droplets to collect on the condensation surface.
  • Cooling the gas stream may comprise cooling the gas stream to about 100 to about 300° F., about 110 to about 289° F., about 120 to about 280° F., about 120 to about 150-F, about 290 to about 314° F., about 316 to about 355° F., about 320 to about 340° F., about 357 to about 364° F., or about 366 to about 427° F.
  • cooling the gas stream comprises cooling the gas stream to about 98.6 to about 314.6° F., about 98.6 to about 212.0° F., or about 122.0 to about 314.6° F.
  • Cooling the gas stream may comprise cooling the gas stream to about 100° F. to about 140° F., about 120° F.
  • Cooling the gas stream may comprise cooling the gas stream to about ⁇ 100 to about ⁇ 50° F., about ⁇ 50 to about ⁇ 25° F., about ⁇ 25 to about 0° F., about 0 to about 25° F., about 25 to about 50° F., about 50 to about 75° F., or about 75 to about 100° F.
  • the method may further comprise heating the gas stream and/or extraction chamber to a temperature higher than the boiling point of at least one molecule of the portion of oil, e.g., thereby facilitating volatilization.
  • a temperature may be, for example, about 315° F., about 356° F., or about 428° F.
  • the temperature higher than the boiling point may be about 300° F., about 305° F., about 310° F., about 315° F., about 320° F., about 325° F., about 330° F., about 335° F., about 340° F., about 345° F., about 350° F., about 355° F., about 360° F., about 365° F., about 370° F., about 375° F., about 380° F., about 385° F., about 390° F., about 395° F., about 400° F., about 405° F., about 410° F., about 415° F., about 420° F., about 425° F., about 430° F., about 435° F., about 440° F., about 445° F., about 450° F., or about 460° F.
  • the at least one molecule may comprise cannabidiol (CBD), cannabidivarin (CBDV), cannabigerol (CBG), delta-9-tetrahydrocannabinol (THC), delta-8-tetrahydrocannabinol, tetrahydrocannabivarin (THCV), cannabinol (CBN), cannabigerol, cannabichromene, a chemically converted cannabinoid, any other cannabinoid, any other terpene or terpenoid, linalool, caryophyllene, myrcene, limonene, humulene, and/or pinene.
  • CBD cannabidiol
  • CBD cannabidivarin
  • CBD cannabigerol
  • THC delta-9-tetrahydrocannabinol
  • THCV delta-8-tetrahydrocannabinol
  • THCV tetrahydro
  • the plant material may comprise hemp or cannabis.
  • the plant material may comprise Cannabis sativa, Cannabis indica, Cannabis ruderalis , a hybridized cross of a species or family of cannabis, or a combination of two or more of the foregoing.
  • the portion of oil and/or collected oil comprises cannabidiol (CBD), cannabidivarin (CBDV), cannabigerol (CBG), delta-9-tetrahydrocannabinol (THC), delta-8-tetrahydrocannabinol, tetrahydrocannabivarin (THCV), cannabinol (CBN), cannabigerol, cannabichromene, a chemically converted cannabinoid, any other cannabinoid, any other terpene or terpenoid, linalool, caryophyllene, myrcene, limonene, humulene, pinene, or a combination of two or more of the foregoing.
  • CBD cannabidiol
  • CBD cannabidivarin
  • CBG cannabigerol
  • THC delta-9-tetrahydrocannabinol
  • THCV delta-8-tetrahydrocanna
  • the portion of oil and/or collected oil may comprise delta-9-tetrahydrocannabinol (THC), e.g., at a weight percentage of at least about 10%, 15%, 20%, 25%, 30%, 35%, 40%, 45%, 50%, 55%, 60%, 65%, 70%, 75%, 80%, 85%, 90%, 95%, or about 99%.
  • the portion of oil and/or collected oil may comprise cannabidiol (CBD), e.g., at a weight percentage of at least about 10%, 15%, 20%, 25%, 30%, 35%, 40%, 45%, 50%, 55%, 60%, 65%, 70%, 75%, 80%, 85%, 90%, 95%, or about 99%.
  • CBD cannabidiol

Landscapes

  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Wood Science & Technology (AREA)
  • Extraction Or Liquid Replacement (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Fats And Perfumes (AREA)
  • Separating Particles In Gases By Inertia (AREA)
US16/098,265 2016-05-02 2017-05-02 Method and apparatus for extracting botanical oils Active US10617974B2 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
US16/098,265 US10617974B2 (en) 2016-05-02 2017-05-02 Method and apparatus for extracting botanical oils

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
US201662330522P 2016-05-02 2016-05-02
US16/098,265 US10617974B2 (en) 2016-05-02 2017-05-02 Method and apparatus for extracting botanical oils
PCT/US2017/030557 WO2017192527A1 (fr) 2016-05-02 2017-05-02 Procédé et appareil améliorés d'extraction d'huiles botaniques

Related Parent Applications (1)

Application Number Title Priority Date Filing Date
PCT/US2017/030557 A-371-Of-International WO2017192527A1 (fr) 2016-05-02 2017-05-02 Procédé et appareil améliorés d'extraction d'huiles botaniques

Related Child Applications (1)

Application Number Title Priority Date Filing Date
US16/843,680 Continuation US20200246722A1 (en) 2016-05-02 2020-04-08 Method and apparatus for extracting botanical oils

Publications (2)

Publication Number Publication Date
US20190151771A1 US20190151771A1 (en) 2019-05-23
US10617974B2 true US10617974B2 (en) 2020-04-14

Family

ID=60203273

Family Applications (2)

Application Number Title Priority Date Filing Date
US16/098,265 Active US10617974B2 (en) 2016-05-02 2017-05-02 Method and apparatus for extracting botanical oils
US16/843,680 Pending US20200246722A1 (en) 2016-05-02 2020-04-08 Method and apparatus for extracting botanical oils

Family Applications After (1)

Application Number Title Priority Date Filing Date
US16/843,680 Pending US20200246722A1 (en) 2016-05-02 2020-04-08 Method and apparatus for extracting botanical oils

Country Status (9)

Country Link
US (2) US10617974B2 (fr)
EP (1) EP3452195A4 (fr)
JP (1) JP7020634B2 (fr)
CN (1) CN109310931A (fr)
AU (1) AU2017259422A1 (fr)
BR (1) BR112018072520A2 (fr)
CA (1) CA3022633A1 (fr)
IL (1) IL262703A (fr)
WO (1) WO2017192527A1 (fr)

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10974164B1 (en) 2019-10-10 2021-04-13 Boulder Creek Technologies, LLC Continuous biomass extraction system and process
US11221180B2 (en) 2019-04-02 2022-01-11 Innovative Environmental Companies, Inc. Systems and methods related to staged drying of temperature sensitive materials
US11224825B2 (en) * 2018-10-23 2022-01-18 George Stantchev Separation system and method thereof
US11406913B2 (en) 2013-10-04 2022-08-09 Natural Extraction Systems, LLC Method and apparatus for extracting botanical oils
US20230124244A1 (en) * 2021-10-17 2023-04-20 George Stantchev Extraction apparatus and method thereof
US11643402B2 (en) 2018-08-10 2023-05-09 Natural Extraction Systems, LLC Gas phase methods to decarboxylate cannabinoids
US11702397B2 (en) 2018-08-10 2023-07-18 Natural Extraction Systems, LLC Methods to purify cannabinoids
US11938415B2 (en) 2020-12-01 2024-03-26 Jaxon Technologies, LLC Processes and systems for recovery of solvents and target botanical compounds

Families Citing this family (38)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10239808B1 (en) 2016-12-07 2019-03-26 Canopy Holdings, LLC Cannabis extracts
JP7225104B2 (ja) 2017-02-01 2023-02-20 ジービーエス グローバル バイオファーマ，インコーポレイテッド マスト細胞関連炎症障害又は好塩基球媒介炎症障害の治療のためのカンナビノイド含有複合混合物
US10272360B2 (en) 2017-08-05 2019-04-30 Priya Naturals, Inc. Phytochemical extraction system and methods to extract phytochemicals from plants including plants of the family Cannabaceae sensu stricto
US10596486B2 (en) * 2017-09-21 2020-03-24 Louis Phillip Nevitt Plant matter fractional distillation system using heated air induction into precisely heated chamber to extract a plant's organic compounds without use of solvents
IL255268B (en) * 2017-10-26 2019-01-31 Izun Pharmaceuticals Corp Smoke capture system and method
US10933390B2 (en) * 2017-12-13 2021-03-02 Wisys Technology Foundation, Inc. Microparticle generation system
EP3745884A1 (fr) 2018-01-31 2020-12-09 Canopy Holdings, Llc Poudre de chanvre
US20190308116A1 (en) * 2018-04-10 2019-10-10 Craig Alan Brodersen Solvent based cannabinoid extraction process with improved efficiency, safety, quality, which yields a homogenous and pasteurized product
AU2019277283B2 (en) 2018-05-30 2021-10-28 Botanical Extraction Solvent Free Ltd. System and method for extracting and separating botanical oils without the use of solvents
CA3006692A1 (fr) * 2018-05-30 2019-11-30 Kevin Allan Dooley Inc. Un systeme et une methode d'extraction et de separation d'huiles botaniques sans utilisation de solvants
CA3119729A1 (fr) 2018-10-10 2020-04-16 Treehouse Biotech, Inc. Synthese du cannabigerol
WO2020106920A1 (fr) * 2018-11-21 2020-05-28 Priya Naturals, Inc. Procédés et systèmes exempts de solvant pour l'extraction de produits phytochimiques à partir de plantes comprenant des plantes de cannabacées
EP3887056A4 (fr) * 2018-11-27 2022-10-12 VortX Kleanair Systems Filtre à eau de flux d'échappement à température régulée pour des machines à café
US20220015397A1 (en) * 2018-12-10 2022-01-20 Natural Extraction Systems, LLC Compositions with novel cannabinoid and terpene profiles
CN111820449B (zh) * 2019-04-15 2021-07-27 云南汉盟制药有限公司 一种从工业大麻中提取挥发油的方法
AU2020296487A1 (en) * 2019-06-21 2022-01-20 Hexo Operations Inc. Industrial-scale processing of cannabis material
EP4017950A4 (fr) 2019-08-20 2023-09-13 Craig, Scott, E. Appareil et procédé d'extraction d'huiles essentielles
US20230190670A1 (en) * 2019-12-02 2023-06-22 Natural Extraction Systems, LLC Compositions comprising novel cannabinoid and terpene profiles
US11813833B2 (en) 2019-12-09 2023-11-14 Owens Corning Intellectual Capital, Llc Fiberglass insulation product
US20210170302A1 (en) * 2019-12-10 2021-06-10 Loxley Systems, Llc Systems, methods, and equipment for chemical extraction
CA3167368A1 (fr) * 2020-02-09 2021-08-12 C. Russell Thomas Procedes en phase gazeuse pour extraire des produits naturels
CA3169774A1 (fr) * 2020-02-27 2021-09-02 Robert N. WIRTZ Appareil et procede pour extraire de l'huile d'une matiere vegetale
CN111302900B (zh) * 2020-04-02 2022-07-12 广西宝汇佳利投资管理有限公司 一种有机溶剂气提法萃取大麻二酚的方法
US11504644B2 (en) * 2020-07-02 2022-11-22 Colorado Extraction Systems, LLC Closed loop extraction system
CA3201543A1 (fr) * 2020-12-10 2022-06-16 Clancy CALLAGHAN Systemes, dispositifs et procedes pour echange de chaleur en cycle ferme symphasique
AU2021411968A1 (en) 2020-12-31 2023-07-13 Cookies Creative Consulting & Promotions, Inc. Compositions comprising cannabis and mushroom extracts, and uses thereof
EP4288175A1 (fr) * 2021-02-04 2023-12-13 Python Extraction Systems, LLC Système d'extraction de terpènes et procédé d'extraction de terpènes à partir de biomasse végétale
WO2022173789A1 (fr) * 2021-02-10 2022-08-18 Natural Extraction Systems, LLC Cannabigérol et dérivés de cannabigérol destinés à être utilisés pour traiter des états de santé chez l'homme
WO2022213109A2 (fr) 2021-03-31 2022-10-06 Rj Lee Group, Inc. Procédés d'isolement et de purification de cannabidiol (cbd) et de terpènes à partir de chanvre
CN113308302A (zh) * 2021-04-26 2021-08-27 杨天宇 提取物料有效成分的系统
WO2022251329A1 (fr) * 2021-05-25 2022-12-01 Central Coast Agriculture, Inc. Systèmes et procédés d'extraction de matériaux
GB2610556A (en) * 2021-09-02 2023-03-15 113 Botanicals Ltd Extraction
CN113812667B (zh) * 2021-09-27 2023-05-05 浙江中烟工业有限责任公司 一种烟草致香成分干馏提取装备及方法
CN114042355B (zh) * 2021-09-27 2023-03-21 浙江中烟工业有限责任公司 烟叶原料流化床干馏产物过滤系统及其旋风分离工艺
CN113876021B (zh) * 2021-09-27 2023-06-16 浙江中烟工业有限责任公司 一种烟叶提取致香冷凝液的方法及其致香冷凝液
CN115068974B (zh) * 2022-05-16 2024-03-26 深圳昱朋科技有限公司 一种植物香料的制备方法
WO2023250274A1 (fr) 2022-06-22 2023-12-28 Ilera Therapeutics Llc Matrice de capture et de dissolution améliorée pour cannabinoïdes et leurs procédés de fabrication
WO2024015780A1 (fr) 2022-07-11 2024-01-18 Ilera Therapeutics Llc Zlt-007 et méthodes de traitement de la neuropathie diabétique

Citations (42)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2467435A (en) 1944-08-25 1949-04-19 Anderson Co V D Solvent recovery distillation system
GB635121A (en) 1945-01-25 1950-04-05 Germinal S A Improvements in or relating to the preparation of extracts from aromatic plants
US2805981A (en) 1953-03-20 1957-09-10 Phillips Petroleum Co Process and apparatus for flash distillation
US3270437A (en) 1963-04-22 1966-09-06 Lara Carlos Castillo Continuous operation vegetable matter essence extraction apparatus
US4227997A (en) 1978-12-14 1980-10-14 Peabody-Myers Corporation Mobile non-polluting cleaning and processing apparatus and method
US4279824A (en) 1979-11-01 1981-07-21 Mckinney Laurence O Method and apparatus for processing herbaceous plant materials including the plant cannabis
US4396487A (en) 1980-11-10 1983-08-02 Georgia Oil & Gas Company Process for retorting oil shale and the like
US4752307A (en) 1986-01-21 1988-06-21 Shell Oil Company Contacting gas and liquid
US5026549A (en) 1988-08-26 1991-06-25 Biolandes Technologies Method of extracting solid materials using a solvent and an apparatus for implementing same
US5235992A (en) 1991-06-28 1993-08-17 R. J. Reynolds Tobacco Company Processes for producing flavor substances from tobacco and smoking articles made therewith
US5408924A (en) 1992-06-19 1995-04-25 Food Sciences, Inc. Apparatus for the extraction of edible oils
US6019819A (en) 1998-03-17 2000-02-01 Alpha Engineers, Inc. Apparatus and method for extracting heat from contaminated waste steam
US6248910B1 (en) 1991-12-31 2001-06-19 University Research & Marketing Inc. Process for extracting oil from oil-bearing naturally occurring organic materials
US6403126B1 (en) 1999-05-26 2002-06-11 Websar Innovations Inc. Cannabinoid extraction method
US20020139097A1 (en) * 2001-03-30 2002-10-03 Stephane Brilmaker Centrifugal particulate matter gas separator
US20040049059A1 (en) 2000-10-17 2004-03-11 Adam Mueller Method for producing an extract from cannabis plant matter, containing a tetrahydrocannabinol and a cannabidiol and cannabis extracts
US20040147769A1 (en) 2002-01-08 2004-07-29 Davis John Henry Oil extraction process and apparatus therefor
US20040147767A1 (en) 2001-05-04 2004-07-29 Brian Whittle Processes and apparatus for extraction of active substances and enriched extracts from natural products
US6860998B1 (en) 1999-08-05 2005-03-01 Naturol Limited Process and apparatus for preparing extracts and oils from plants and other matter
US20050172802A1 (en) * 2002-04-29 2005-08-11 Shell Oil Company Supersonic fluid separation enhanced by spray injection
US7001502B1 (en) 1998-09-29 2006-02-21 Canadian Enviromnental Equipment & Engineering Technologies, Inc. Process for treating crude oil using hydrogen in a special unit
US7344736B2 (en) 2002-08-14 2008-03-18 Gw Pharma Limited Extraction of pharmaceutically active components from plant materials
US20090054711A1 (en) 2005-05-04 2009-02-26 Tom Lawrence Pyrolysis Systems, Methods of Use Thereof, and Methods of Bio-Oil Transformation
CN101553702A (zh) 2006-12-06 2009-10-07 普莱克斯技术有限公司 分离方法及装置
JP4388715B2 (ja) 2001-05-14 2009-12-24 光彦 棚橋 植物由来抽出物の抽出方法及びその抽出装置
US7833298B2 (en) 2005-06-10 2010-11-16 Fmc Technologies C.V. System and inlet device for separating a mixture
CN201643760U (zh) 2010-04-20 2010-11-24 湖北俊辉药业有限公司 一种蒸汽提取器
US20110119606A1 (en) * 2009-11-17 2011-05-19 Canon Kabushiki Kaisha Information processing apparatus and method thereof
US20110133120A1 (en) 2009-06-05 2011-06-09 Mcghee David Plant oil extraction
US8062410B2 (en) 2004-10-12 2011-11-22 Great River Energy Apparatus and method of enhancing the quality of high-moisture materials and separating and concentrating organic and/or non-organic material contained therein
JP4849578B1 (ja) 2010-07-29 2012-01-11 兼松エンジニアリング株式会社 マイクロ波を利用した抽出装置
US8329229B2 (en) 2006-12-21 2012-12-11 E I Du Pont De Nemours And Company Steam distillation of catmint plants
US8343553B2 (en) 2011-04-18 2013-01-01 Hospodor Andrew D Essential element extractor
US8445034B1 (en) 2010-11-02 2013-05-21 Albert L Coles, Jr. Systems and methods for producing organic cannabis tincture
US20130240347A1 (en) 2012-03-14 2013-09-19 State University Essential oil extraction apparatus
EP2644039A1 (fr) 2012-03-28 2013-10-02 Helmut Rausche Procédé d'obtention d'arômes à partir de matérial biologique
US20140001027A1 (en) 2012-06-21 2014-01-02 Aromator Llc Distillation apparatus for extraction of essential oils and hydrosols from plant matter within a capsule
WO2014000077A1 (fr) 2012-06-26 2014-01-03 Universidade Federal De Ouro Preto - Ufop Procédé d'obtention en hautes concentration du constituant chimique trans-pinocarvyl acétate par hydrodistillation des parties aériennes de microlicia graveolens et obtention de formulations nanoémulsionnées
US20140113010A1 (en) 2012-10-18 2014-04-24 Andrew D. Hospodor Essential Element Management
US20140193303A1 (en) 2013-01-04 2014-07-10 Matthew A. Ellis Apparatus for Extracting Oil From Oil-Bearing Plant Material
WO2015049585A2 (fr) 2013-10-04 2015-04-09 Natural Extraction Services, Llc Procédé et appareil pour extraire des huiles botaniques
US20150252286A1 (en) 2009-11-11 2015-09-10 E. I. Du Pont De Nemours And Company Method for isolation of catmint oil

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5112455A (en) * 1974-07-22 1976-01-31 Yasunaga Riken Co Ltd Kansohoho oyobi sochi
JPS51104476A (ja) * 1975-03-13 1976-09-16 Kochiwa Seisakusho Kk Kiekisetsushokuhohooyobisochi
US5516923A (en) * 1992-04-27 1996-05-14 Agritech International Extracting oil from oil bearing plant parts
US9358259B2 (en) * 2012-03-20 2016-06-07 Andrew David Hospodor Recycling cannabinoid extractor
CN103357193B (zh) * 2012-03-26 2015-06-10 侯梦斌 一种介入过热蒸汽的植物提取物生产设备与工艺
CN203458833U (zh) * 2013-09-18 2014-03-05 宁波大学 连续式提取、浓缩、干燥生产线

Patent Citations (45)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2467435A (en) 1944-08-25 1949-04-19 Anderson Co V D Solvent recovery distillation system
GB635121A (en) 1945-01-25 1950-04-05 Germinal S A Improvements in or relating to the preparation of extracts from aromatic plants
US2805981A (en) 1953-03-20 1957-09-10 Phillips Petroleum Co Process and apparatus for flash distillation
US3270437A (en) 1963-04-22 1966-09-06 Lara Carlos Castillo Continuous operation vegetable matter essence extraction apparatus
US4227997A (en) 1978-12-14 1980-10-14 Peabody-Myers Corporation Mobile non-polluting cleaning and processing apparatus and method
US4279824A (en) 1979-11-01 1981-07-21 Mckinney Laurence O Method and apparatus for processing herbaceous plant materials including the plant cannabis
US4396487A (en) 1980-11-10 1983-08-02 Georgia Oil & Gas Company Process for retorting oil shale and the like
US4752307A (en) 1986-01-21 1988-06-21 Shell Oil Company Contacting gas and liquid
US5026549A (en) 1988-08-26 1991-06-25 Biolandes Technologies Method of extracting solid materials using a solvent and an apparatus for implementing same
US5235992A (en) 1991-06-28 1993-08-17 R. J. Reynolds Tobacco Company Processes for producing flavor substances from tobacco and smoking articles made therewith
US6248910B1 (en) 1991-12-31 2001-06-19 University Research & Marketing Inc. Process for extracting oil from oil-bearing naturally occurring organic materials
US5408924A (en) 1992-06-19 1995-04-25 Food Sciences, Inc. Apparatus for the extraction of edible oils
US6019819A (en) 1998-03-17 2000-02-01 Alpha Engineers, Inc. Apparatus and method for extracting heat from contaminated waste steam
US7001502B1 (en) 1998-09-29 2006-02-21 Canadian Enviromnental Equipment & Engineering Technologies, Inc. Process for treating crude oil using hydrogen in a special unit
US6403126B1 (en) 1999-05-26 2002-06-11 Websar Innovations Inc. Cannabinoid extraction method
US6860998B1 (en) 1999-08-05 2005-03-01 Naturol Limited Process and apparatus for preparing extracts and oils from plants and other matter
US20040049059A1 (en) 2000-10-17 2004-03-11 Adam Mueller Method for producing an extract from cannabis plant matter, containing a tetrahydrocannabinol and a cannabidiol and cannabis extracts
US20020139097A1 (en) * 2001-03-30 2002-10-03 Stephane Brilmaker Centrifugal particulate matter gas separator
US20040147767A1 (en) 2001-05-04 2004-07-29 Brian Whittle Processes and apparatus for extraction of active substances and enriched extracts from natural products
US20100119606A1 (en) 2001-05-04 2010-05-13 Gw Pharma Limited Processes and apparatus for extraction of active substances and enriched extracts from natural products
US7622140B2 (en) 2001-05-04 2009-11-24 Gw Pharma Limited Processes and apparatus for extraction of active substances and enriched extracts from natural products
JP4388715B2 (ja) 2001-05-14 2009-12-24 光彦 棚橋 植物由来抽出物の抽出方法及びその抽出装置
US20040147769A1 (en) 2002-01-08 2004-07-29 Davis John Henry Oil extraction process and apparatus therefor
US20050172802A1 (en) * 2002-04-29 2005-08-11 Shell Oil Company Supersonic fluid separation enhanced by spray injection
US7344736B2 (en) 2002-08-14 2008-03-18 Gw Pharma Limited Extraction of pharmaceutically active components from plant materials
US8062410B2 (en) 2004-10-12 2011-11-22 Great River Energy Apparatus and method of enhancing the quality of high-moisture materials and separating and concentrating organic and/or non-organic material contained therein
US20090054711A1 (en) 2005-05-04 2009-02-26 Tom Lawrence Pyrolysis Systems, Methods of Use Thereof, and Methods of Bio-Oil Transformation
US7833298B2 (en) 2005-06-10 2010-11-16 Fmc Technologies C.V. System and inlet device for separating a mixture
US9038413B2 (en) 2006-12-06 2015-05-26 Praxair Technology, Inc. Separation method and apparatus
CN101553702A (zh) 2006-12-06 2009-10-07 普莱克斯技术有限公司 分离方法及装置
US8329229B2 (en) 2006-12-21 2012-12-11 E I Du Pont De Nemours And Company Steam distillation of catmint plants
US20110133120A1 (en) 2009-06-05 2011-06-09 Mcghee David Plant oil extraction
US20150252286A1 (en) 2009-11-11 2015-09-10 E. I. Du Pont De Nemours And Company Method for isolation of catmint oil
US20110119606A1 (en) * 2009-11-17 2011-05-19 Canon Kabushiki Kaisha Information processing apparatus and method thereof
CN201643760U (zh) 2010-04-20 2010-11-24 湖北俊辉药业有限公司 一种蒸汽提取器
JP4849578B1 (ja) 2010-07-29 2012-01-11 兼松エンジニアリング株式会社 マイクロ波を利用した抽出装置
US8445034B1 (en) 2010-11-02 2013-05-21 Albert L Coles, Jr. Systems and methods for producing organic cannabis tincture
US8343553B2 (en) 2011-04-18 2013-01-01 Hospodor Andrew D Essential element extractor
US20130240347A1 (en) 2012-03-14 2013-09-19 State University Essential oil extraction apparatus
EP2644039A1 (fr) 2012-03-28 2013-10-02 Helmut Rausche Procédé d'obtention d'arômes à partir de matérial biologique
US20140001027A1 (en) 2012-06-21 2014-01-02 Aromator Llc Distillation apparatus for extraction of essential oils and hydrosols from plant matter within a capsule
WO2014000077A1 (fr) 2012-06-26 2014-01-03 Universidade Federal De Ouro Preto - Ufop Procédé d'obtention en hautes concentration du constituant chimique trans-pinocarvyl acétate par hydrodistillation des parties aériennes de microlicia graveolens et obtention de formulations nanoémulsionnées
US20140113010A1 (en) 2012-10-18 2014-04-24 Andrew D. Hospodor Essential Element Management
US20140193303A1 (en) 2013-01-04 2014-07-10 Matthew A. Ellis Apparatus for Extracting Oil From Oil-Bearing Plant Material
WO2015049585A2 (fr) 2013-10-04 2015-04-09 Natural Extraction Services, Llc Procédé et appareil pour extraire des huiles botaniques

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11406913B2 (en) 2013-10-04 2022-08-09 Natural Extraction Systems, LLC Method and apparatus for extracting botanical oils
US11643402B2 (en) 2018-08-10 2023-05-09 Natural Extraction Systems, LLC Gas phase methods to decarboxylate cannabinoids
US11702397B2 (en) 2018-08-10 2023-07-18 Natural Extraction Systems, LLC Methods to purify cannabinoids
US11224825B2 (en) * 2018-10-23 2022-01-18 George Stantchev Separation system and method thereof
US11221180B2 (en) 2019-04-02 2022-01-11 Innovative Environmental Companies, Inc. Systems and methods related to staged drying of temperature sensitive materials
US10974164B1 (en) 2019-10-10 2021-04-13 Boulder Creek Technologies, LLC Continuous biomass extraction system and process
US11624038B2 (en) 2019-10-10 2023-04-11 Boulder Creek Technologies, LLC Continuous biomass extraction system and process
US11938415B2 (en) 2020-12-01 2024-03-26 Jaxon Technologies, LLC Processes and systems for recovery of solvents and target botanical compounds
US20230124244A1 (en) * 2021-10-17 2023-04-20 George Stantchev Extraction apparatus and method thereof
US11766629B2 (en) * 2021-10-17 2023-09-26 George Stantchev Extraction apparatus and method thereof

Also Published As

Publication number Publication date
EP3452195A1 (fr) 2019-03-13
JP7020634B2 (ja) 2022-02-16
JP2019518590A (ja) 2019-07-04
US20200246722A1 (en) 2020-08-06
US20190151771A1 (en) 2019-05-23
IL262703A (en) 2018-12-31
CA3022633A1 (fr) 2017-11-09
EP3452195A4 (fr) 2020-01-22
WO2017192527A1 (fr) 2017-11-09
AU2017259422A1 (en) 2018-11-15
CN109310931A (zh) 2019-02-05
BR112018072520A2 (pt) 2019-03-19

Similar Documents

Publication Publication Date Title
US20200246722A1 (en) Method and apparatus for extracting botanical oils
EP3283606B1 (fr) Procédé et appareil améliorés d'extraction d'huiles botaniques
US10881982B2 (en) Method and apparatus for extracting botanical oils
US3300868A (en) Process for drying heat-sensitive materials as well as drying apparatus for the performance of the aforementioned process
TWI708762B (zh) 用於在不使用溶劑的情況下萃取和分離植物油的系統和方法
GB2372714A (en) Distillation of volatile constituent from plant material without use of solvent
US20230242839A1 (en) Continuous biomass extraction system and process
RU2356632C1 (ru) Фильтр очистки газового потока
US4278450A (en) Method for the recovery of clean pyrolysis off-gas and a rotary recycling means therefor
RU2715944C1 (ru) Способ охлаждения воздуха в теплообменном аппарате и теплообменный аппарат
BG4354U1 (bg) Инсталация за непрекъсната екстракция на масла и вторични метаболити от растителни суровини
CN105854329A (zh) 制备聚乙烯低聚物粉末的“精馏+冷冻喷雾”干燥方法

Legal Events

Date Code Title Description
FEPP Fee payment procedure

Free format text: ENTITY STATUS SET TO UNDISCOUNTED (ORIGINAL EVENT CODE: BIG.); ENTITY STATUS OF PATENT OWNER: SMALL ENTITY

AS Assignment

Owner name: NATURAL EXTRACTION SYSTEMS, LLC, COLORADO

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:THOMAS, C. RUSSELL;REEL/FRAME:047396/0101

Effective date: 20181030

FEPP Fee payment procedure

Free format text: ENTITY STATUS SET TO SMALL (ORIGINAL EVENT CODE: SMAL); ENTITY STATUS OF PATENT OWNER: SMALL ENTITY

AS Assignment

Owner name: NATURAL EXTRACTION SYSTEMS, LLC, COLORADO

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:THOMAS, C. RUSSELL;REEL/FRAME:047797/0699

Effective date: 20181030

STPP Information on status: patent application and granting procedure in general

Free format text: NON FINAL ACTION MAILED

STPP Information on status: patent application and granting procedure in general

Free format text: RESPONSE TO NON-FINAL OFFICE ACTION ENTERED AND FORWARDED TO EXAMINER

STPP Information on status: patent application and granting procedure in general

Free format text: NOTICE OF ALLOWANCE MAILED -- APPLICATION RECEIVED IN OFFICE OF PUBLICATIONS

STCF Information on status: patent grant

Free format text: PATENTED CASE

FEPP Fee payment procedure

Free format text: MAINTENANCE FEE REMINDER MAILED (ORIGINAL EVENT CODE: REM.); ENTITY STATUS OF PATENT OWNER: SMALL ENTITY

FEPP Fee payment procedure

Free format text: SURCHARGE FOR LATE PAYMENT, SMALL ENTITY (ORIGINAL EVENT CODE: M2554); ENTITY STATUS OF PATENT OWNER: SMALL ENTITY

MAFP Maintenance fee payment

Free format text: PAYMENT OF MAINTENANCE FEE, 4TH YR, SMALL ENTITY (ORIGINAL EVENT CODE: M2551); ENTITY STATUS OF PATENT OWNER: SMALL ENTITY

Year of fee payment: 4